Mediated electrochemical oxidation of destruction of sharps

ABSTRACT

Sharps are introduced into an apparatus for contacting the sharps with an electrolyte containing the oxidized form of one or more reversible redox couples, at least one of which is produced electrochemically by anodic oxidation at the anode of an electrochemical cell. The oxidized forms of any other redox couples present are produced either by similar anodic oxidation or reaction with the oxidized form of other redox couples present and capable of affecting the required redox reaction. The oxidized species of the redox couples oxidize sharps and the biological waste on the sharps and are themselves converted to their reduced form, whereupon they are reoxidized by either of the aforementioned mechanisms and the redox cycle continues until all oxidizable waste species, including intermediate reaction products, have undergone the desired degree of oxidation. The entire process takes place at temperatures between ambient and approximately 100° C. The oxidation process will be enhanced by the addition of reaction enhancements, such as: ultrasonic energy and/or ultraviolet radiation.

FIELD OF THE INVENTION

This invention relates generally to a process and apparatus for themediated electrochemical oxidation (MEO) destruction and/orsterilization of sharps that have been used in animal or human patientcare or treatment or in medical, research, or industrial laboratories.

In this patent there is a distinction between the sharps that can bedestroyed and those that can be sterilized. Those that can be destroyedincludes, but is not limited to, hypodermic needles, syringes, scalpelblades, needles with attached tubing, suture needles, razor blades,disposable razors, disposable scissors (used in surgery, labor anddelivery, or other medical procedures), intravenous stylets and rigidintroducers (e.g., J wires), tattoo needles, acupuncture needles,electrolysis needles, disposal plastic surgery instruments, plasticitems (with the exception of PTFEs) and combined waste (e.g. a mixtureof any of the foregoing with each other or other non-biological waste)henceforth collectively referred to as ‘Sharps I’.

A broader definition of sharps is “objects or devices having acute rigidcorners, edges points or protuberances capable of cutting or penetratingthe skin”. In this expanded definition materials made out of glass orPTFE are added to the aforementioned classes. The MEO process andapparatus in this patent destroys all the materials (i.e., sterilizingand disinfecting) remaining on glass and PTFE items from their use inanimal or human patient care or treatment or in medical, research, orindustrial laboratories, which includes, but is not limited to, brokenglass and/or glassware, slides, cover slips, Pasteur pipettes, bloodvials, glass tubing, and PTFE products broken or intact. These objectsare referred to as ‘Sharps II’ and the combination of ‘Sharps I’ and‘Sharps II’ will be referred to as ‘Sharps III’. The term sharp is usedas a generic term not distinguishing between the three defined groups.

During the use of the sharps, materials from the contact with humans oranimals remain on the surface of the sharps. The materials arebiological waste and may be infectious and contain pathogenic substancesas well as all types of microbial material. For purposes of this patentthe materials remaining on the sharps will be referred to as biologicalwaste.

The following documents are added to the definition so as to furtherclarify the scope and definition of biological waste as any waste thatis considered by any of, but not limited to, the following statutes andregulations:

-   -   New Jersey State Statute, “Comprehensive Regulatory Medical        Waste Management Act”, P.L. 1989, c. 34 (C.13.1E-48.13).    -   New York State Environmental Conservation Law, TITLE 15,        “STORAGE, TREATMENT, DISPOSAL AND TRANSPORTATION OF REGULATED        MEDICAL WASTE”, Section 27-1501. Definitions.    -   New York State Public Health Law, TITLE XIII, “STORAGE,        TREATMENT AND DISPOSAL OF REGULATED MEDICAL WASTE”, Section        1389-aa. Definitions.    -   CALIFORNIA HEALTH AND SAFETY CODE, SECTION 117635. “Biohazardous        Waste” Title 25 Health Services, Part I.    -   Texas Department of Health, Chapter 1 Texas Board of Health,        “Definition, Treatment, and Disposition of Special Waste from        Health Care-Related Facilities, Section 1.132 Definitions.    -   40 C.F.R. 60.51(c) PROTECTION OF ENVIRONMENT; Standards of        performance for new stationary sources.    -   40 C.F.R. 240.101 PROTECTION OF ENVIRONMENT; Guidelines for the        thermal processing of solid wastes (Section P only).    -   49 C.F.R. 173.134 TRANSPORTATION; Class 6, Division        6.2-Definitions, exceptions and packing group assignments.    -   33 C.F.R. 151.05 TITLE 33□□NAVIGATION AND NAVIGABLE WATERS;        VESSELS CARRYING OIL, NOXIOUS LIQUID SUBSTANCES, GARBAGE,        MUNICIPAL OR COMMERCIAL WASTE, AND BALLAST WATER□; Definitions        (medical waste only).

Relative to the use of sharps throughout this patent the author meansdestruction of the sharp unless the discussion includes glass and PTFEitems in which case it means the sterilization of those items.

The foregoing list of State statutes and United States FederalRegulations are overlapping but are necessary to accurately define thematerials since no single statute or regulation covers all the materialsfor which this invention applies.

BACKGROUND OF THE INVENTION

The disposal of sharps and their biological waste in the U.S. is amulti-million dollar per year industry. The capital cost of theequipment required is in the tens of millions of dollars. Allinstitutions and businesses that generate and handle sharps must providesafe effective and inexpensive disposal of the sharps. In recent yearsthere has been increasing concern over the disposal of sharps. The twoprinciple methodologies for the disposal of sharps are incineration anddumping in landfills. Incinerated sharps potentially produce hazardousemissions and still maintain their recognizable shape which are viewedby the general public as dangerous items. Most landfills have institutedrules for the acceptance of any medical waste that require the sharps tobe preprocessed to the point where they are not recognizable as sharps.Placing of sharps into especially designed containers to protect thehandling of sharps during the disposal process is generally a statutoryrequirement. Medical and veterinary communities, business and privateuse of sharps are in need of improved methods of handling, destroying,and/or sterilizing sharps and their biological waste.

SUMMARY OF THE INVENTION

The invention relates to a method and apparatus for the mediatedelectrochemical oxidation (MEO) destruction and/or sterilization ofsharps that have been used in animal or human patient care or treatmentor in medical, research, or industrial laboratories.

In this patent there is a distinction between the sharps that can bedestroyed and those that can be sterilized. Those that can be destroyedwhich includes, but is not limited to, hypodermic needles, syringes,scalpel blades, needles with attached tubing, suture needles, razorblades, disposable razors, disposable scissors (used in surgery, laborand delivery, or other medical procedures), intravenous stylets andrigid introducers (e.g., J wires), tattoo needles, acupuncture needles,electrolysis needles, disposal plastic surgery instruments, plasticitems (with the exception of PTFEs) and combined waste (e.g. a mixtureof any of the foregoing with each other or other non-biological waste)henceforth collectively referred to as ‘Sharps I’.

A broader definition of sharps is “objects or devices having acute rigidcorners, edges points or protuberances capable of cutting or penetratingthe skin”. In this expanded definition materials made out of glass orPTFE are added to the aforementioned classes. The MEO process andapparatus in this patent destroys all the materials (i.e., sterilizingand disinfecting) remaining on glass and PTFE items from their use inanimal or human patient care or treatment or in medical, research, orindustrial laboratories, which includes, but is not limited to, brokenglass and/or glassware, slides, cover slips, Pasteur pipettes, bloodvials, glass tubing, and PTFE products broken or intact. These objectsare referred to as ‘Sharps II’ and the combination of ‘Sharps I’ and‘Sharps II’ will be referred to as ‘Sharps III’. The term sharps is usedas a generic term not distinguishing between the three defined groups.

During the use of the sharps, materials from contact with humans oranimals may remain on the surface of the sharps. The materials arebiological waste and may be infectious and contain pathogenic substancesas well as all types of microbial material. For purposes of this patentthe materials remaining on the sharps will be referred to as biologicalwaste.

Relative to the use of Sharps I throughout this patent the author meansdestruction of the sharps unless the discuss includes Sharps II andSharps III items in which case it means the sterilization of thoseitems.

The MEO process has been tested using a whole small animal (dead) mouse.After the MEO process had run for a suitable time the physical structureof the mouse was totally converted into a liquid. The liquid was testedand only a very small amount of total carbon content was detected. Thecarbon content of the largest detected hydrocarbon molecules was lessthen thirty (30) carbons per molecule. This result supports theconclusion that the contents of the liquid were sterile/disinfected. Themicroorganism tests to determine the existence of microorganism will becompleted following accepted protocols to substantiate the conclusionthat the MEO process sterilizes and/or disinfects Sharps I and II.

The mediated electrochemical oxidation process involves an electrolytecontaining one or more redox couples, wherein the oxidized form of atleast one redox couple is produced by anodic oxidation at the anode ofan electrochemical cell. The oxidized forms of any other redox couplespresent are produced either by similar anodic oxidation or reaction withthe oxidized form of other redox couples present capable of affectingthe required redox reaction. The oxidized species of the redox couplesoxidize Sharps I and the biological waste molecules residing on thesharps and are themselves converted to their reduced form, whereuponthey are reoxidized by either of the aforementioned mechanisms and theredox cycle continues until all oxidizable species, includingintermediate reaction products, have undergone the desired degree ofoxidation. The redox species ions are thus seen to “mediate” thetransfer of electrons from the sharps (including waste remains on thesharps) to the anode, (i.e., oxidation of the waste). A membrane in theelectrochemical cell separates the anolyte and catholyte, therebypreventing parasitic reduction of the oxidizing species at the cathode.

The preferred MEO process uses the mediator species described in Table I(simple anions redox couple mediators); the Type I isopolyanions (IPA)formed by Mo, W, V, Nb, and Ta, and mixtures there of; the Type Iheteropolyanions (HPA) formed by incorporation into the aforementionedisopolyanions of any of the elements listed in Table II (heteroatoms)either singly or in combinations there of; any type heteropolyanioncontaining at least one heteropolyatom (i.e. element) contained in bothTable I and Table II; or combinations of mediator species from any orall of these generic groups.

Simple Anion Redox Couple Mediators

Table I show the simple anion redox couple mediators used in thepreferred MEO process wherein “species” defines the specific ions foreach chemical element that have applicability to the MEO process aseither the reduced (e.g., BrO₃ ⁻¹) or oxidizer (e.g., BrO₄ ⁻¹) form ofthe mediator characteristic element (e.g., Br), and the “specific redoxcouple” defines the specific associations of the reduced and oxidizedforms of these species (e.g., BrO₃ ⁻¹/BrO₄ ⁻¹) that are claimed for theMEO process. Species soluble in the anolyte are shown in Table I innormal print while those that are insoluble are shown in bold underlinedprint. The characteristics of the MEO Process claimed in this patent arespecified in the following paragraphs.

The anolyte contains one or more redox couples which in their oxidizedform consist of either single multivalent element anions (e.g., Ag⁺²,Ce⁺⁴, Co⁺³, Pb⁺⁴, etc.), insoluble oxides of multivalent elements (e.g.,PbO₂, CeO₂, PrO₂, etc.), or simple oxoanions (also called oxyanions) ofmultivalent elements (e.g., FeO₄ ⁻², NiO₄ ⁻², BiO₃ ⁻, etc.) called themediator species. The nonoxygen multivalentelement component of themediator is called the characteristic element of the mediator species.We have chosen to group the simple oxoanions with the simple anion redoxcouple mediators rather than with the complex (i.e., polyoxometallate(POM)) anion redox couple mediators discussed in the next section andrefer to them collectively as simple anion redox couple mediators.

In one embodiment of this process both the oxidized and reduced forms ofthe redox couple are soluble in the anolyte. The reduced form of thecouple is anodically oxidized to the oxidized form at the cell anode(s)whereupon it oxidizes the sharp and/or molecules of waste remaining onthe sharp either dissolved in or located on waste particle surfaceswetted by the anolyte, with the concomitant reduction of the oxidizingagent to its reduced form, whereupon the MEO process begins again withthe reoxidation of this. species at the cell anode(s). If other lesspowerful redox couples of this type (i.e., reduced and oxidized formssoluble in anolyte) are present, they too may undergo direct anodicoxidation or the anodically oxidized more powerful oxidizing agent mayoxidize them rather that a sharp or waste molecule. The weaker redoxcouple(s) is selected such that their oxidation potential is sufficientto affect the desired reaction with the sharp and/or waste molecules.The oxidized species of all the redox couples oxidize the Sharps Iand/or waste molecules and are themselves converted to their reducedform, whereupon they are reoxidized by either of the aforementionedmechanisms and the redox cycle continues until all Sharps I andbiological waste species, including intermediate reaction products, haveundergone the desired degree of oxidation. The preferred mode for theMEO process as described in the preceding section is for the redoxcouple species to be soluble in the anolyte in both the oxidized andreduced forms, however this is not the only mode of operation claimedherein. If the reduced form of the redox couple is soluble in theanolyte (e.g., Pb⁺²) but the oxidized form is not (e.g., PbO₂), thefollowing processes are operative. The insoluble oxidizing agent isproduced either as a surface layer on the anode by anodic oxidation, orthroughout the bulk of the anolyte by reacting with the oxidized form ofother redox couples present capable of affecting the required redoxreaction, at least one of which is formed by anodic oxidation. TheSharps I and/or biological waste is either soluble in the anolyte ordispersed therein at a fine particle size, (e.g., emulsion, colloid,etc.) thereby affecting intimate contact with the surface of theinsoluble oxidizing agent (e.g., PbO₂) particles. Upon reaction of thewaste with the oxidizing agent particles, the Sharps I or biologicalwaste is oxidized and the insoluble oxidizing agent molecules on theanolyte wetted surfaces of the oxidizing agent particles reacting withthe Sharp I or biological waste are reduced to their soluble form andare returned to the bulk anolyte, available for continuing the MEOprocess by being reoxidized.

In another variant of the MEO process if the reduced form of the redoxcouple is insoluble in the anolyte (e.g., TiO₂) but the oxidized form issoluble (e.g., TiO₂ ⁺²), the following processes are operative. Thesoluble (i.e., oxidized) form of the redox couple is produced by thereaction of the insoluble (i.e., reduced form) redox couple molecules onthe anolyte wetted surfaces of the oxidizing agent particles with thesoluble oxidized form of other redox couples present capable ofaffecting the required redox reaction, at least one of which is formedby anodic oxidation and soluble in the anolyte in both the reduced andoxidized forms. The soluble oxidized species so formed are released intothe anolyte whereupon they oxidize the Sharps I and/or biological wastemolecules in the manner previously described and are themselvesconverted to the insoluble form of the redox couple, thereupon returningto the starting point of the redox MEO cycle.

The electrolytes used in this claim are from a family of acids, alkali,and neutral salt aqueous solutions (e.g. sulfuric acid, potassiumhydroxide, sodium sulfate aqueous solutions etc.).

A given redox couple or mixture of redox couples (i.e. mediator species)will be used with different electrolytes.

The electrolyte composition is selected based on demonstrated adequatesolubility of the compound containing at least one of the mediatorspecies present in the reduced form (e.g., sulfuric acid will be usedwith ferric sulfate, etc.).

The concentration of the mediator species containing compounds in theanolyte will range from 0.0005 molar (M) up to the saturation point.

The concentration of electrolyte in the anolyte will be governed by itseffect upon the solubility of the mediator species containing compoundsand by the conductivity of the anolyte solution desired in theelectrochemical cell for the given mediator species being used.

The temperature over which the electrochemical cell will be operatedwill range from approximately 0° C. too slightly below the boiling pointof the electrolytic solution.

The MEO process is operating at atmospheric pressure.

The mediator species are differentiated on the basis of whether they arecapable of reacting with the electrolyte to produce free radicals (e.g.,•O₂H (perhydroxyl), •OH (hydroxyl), •SO₄ (sulfate), •NO₃ (nitrate),etc.). Such mediator species are classified herein as “super oxidizers”(SO) and typically exhibit oxidation potentials at least equal to thatof the Ce⁺³/Ce⁺⁴ redox couple (i.e., 1.7 volts).

The electrical potential between the electrodes in the electrochemicalcell is based upon the oxidation potential of the most reactive redoxcouple present in the anolyte and serving as a mediator species, and theohmic losses within the cell. Within the current density range ofinterest the electrical potential will be approximately 2.5 to 3.0volts.

Complex Anion Redox Couple Mediators

The preferred characteristic of the oxidizing species in the MEO processis that it be soluble in the aqueous anolyte in both the oxidized andreduced states. The majority of metal oxides and oxoanion (oxyanion)salts are insoluble, or have poorly defined or limited solutionchemistry. The early transition elements, however, are capable ofspontaneously forming a class of discrete polymeric structures calledPOMs (POMs) which are highly soluble in aqueous solutions over a wide pHrange. The polymerization of simple tetrahedral oxoanions of interestherein involves an expansion of the metal, M, coordination number to 6,and the edge and corner linkage of MO₆ octahedra. Chromium is limited toa coordination number of 4, restricting the. POMs based on CrO₄tetrahedra to the dichromate ion [Cr₂O₇]⁻² which is included in Table I.Based upon their chemical composition POMs are divided into the twosubclasses isopolyanions (IPAs) and heteropolyanions (HPAs), as shown bythe following general formulas:Isopolyanions (IPAs)-[M_(m)O_(y)]^(p−)and,Heteropolyanions (HPAs)-[X_(m)M_(m)O_(y)]^(q−)  (m>x)where the addenda atom, M, is usually Molybdenum (Mo) or Tungsten (W),and less frequently Vanadium (V), Niobium (Nb), or Tantalum (Ta), ormixtures of these elements in their highest (d⁰) oxidation state. Theelements that can function as addenda atoms in IPAs and HPAs appear tobe limited to those with both a favorable combination of ionic radiusand charge, and the ability to form dn-pn M—O bonds. However, theheteroatom, X, have no such limitations and can be any of the elementslisted in Table II.

There is a vast chemistry of POMs that involves the oxidation/reductionof the addenda atoms and those heteroatoms listed in Table II thatexhibit multiple oxidation states. The partial reduction of the addenda,M, atoms in some POMs strictures (i.e., both IPAs and HPAs) producesintensely colored species, generically referred to as “heteropolyblues”. Based on structural differences, POMs can be divided into twogroups, Type I and Type II. Type I POMs consist of MO₆ octahedra eachhaving one terminal oxo oxygen atom while Type II have 2 terminal oxooxygen atoms. Type II POMs can only accommodate addenda atoms with d⁰electronic configurations, whereas Type I; e.g., Keggin (XM₁₂O₄₀),Dawson (X₂M₁₈O₆₂), hexametalate (M₆O₁₉), decatungstate (W₁₀O₃₂), etc.,can accommodate addenda atoms with d⁰, d¹, and d² electronicconfigurations. Therefore, while Type I structures can easily undergoreversible redox reactions, structural limitations preclude this abilityin Type II structures. Oxidizing species applicable for the MEO processare therefore Type I POMs (i.e., IPAs and HPAS) where the addenda, M,atoms are W, Mo, V, Nb, Ta, or combinations there of.

The high negative charges of polyanions often stabilize heteroatoms inunusually high oxidation states, thereby creating a second category ofMEO oxidizers in addition to the aforementioned Type I POMs. Any Type Ior Type II HPA containing any of the heteroatom elements, X, listed inTable II, that also are listed in Table I as simple anion redox couplemediators, can also function as an oxidizing species in the MEO process.

The anolytecontains one or more complex anion redox couples, eachconsisting of either the afore mentioned Type I POMs containing W, Mo,V, Nb, Ta or combinations there of as the addenda atoms, or HPAs havingas heteroatoms (X) any elements contained in both Tables I and II, andwhich are soluble in the electrolyte (e.g. sulfuric acid, etc.).

The electrolytes used in this claim are from a family of acids, alkali,and neutral salt aqueous solutions (e.g. sulfuric acid, potassiumhydroxide, sodium sulfate aqueous solutions, etc.).

A given POM redox couple or mixture of POM redox couples (i.e., mediatorspecies) will be used with different electrolytes.

The electrolyte composition is selected based on demonstrating adequatesolubility of at least one of the compounds containing the POM mediatorspecies in the reduced form and being part of a redox couple ofsufficient oxidation potential to affect oxidation of the other mediatorspecies present.

The concentration of the POM mediator species containing compounds inthe anolyte will range from 0.0005M up to the saturation point. Theconcentration of electrolyte in the anolyte will be governed by itseffect upon the solubility of the POM mediator species containingcompounds and by the conductivity of the anolyte solution desired in theelectrochemical cell for the given POM mediator species being used toallow the desired cell current at he desired cell voltage.

The temperature over which the electrochemical cell will be operatedwill range from approximately 0° C. to just below the boiling point ofthe electrolytic solution.

The MEO process is operating at atmospheric pressure.

The POM mediator species are differentiated on the basis of whether theyare capable of reacting with the electrolyte to produce free radicals(e.g., •O₂H, •OH , •SO₄, •NO₃) Such mediator species are classifiedherein as “super oxidizers” (SO) and typically exhibit oxidationpotentials at least equal to that of the Ce⁺³/Ce⁺⁴ redox couple (i.e.,1.7 volts).

The electrical potential between the electrodes in the electrochemicalcell is based on the oxidation potential of the most reactive POM redoxcouple present in the anolyte and serving as a mediator species, and theohmic losses within the cell. Within the current density range ofinterest the electrical potential will be approximately 2.5 to 3.0volts.

Mixed Simple and Complex Anion Redox Couple Mediators

The preferred MEO process for a combination of simple and complex anionredox couple mediators may be mixed together to form the system anolyte.The characteristics of the resulting MEO process is similar to theprevious discussions.

The use of multiple oxidizer species in the MEO process has thefollowing potential advantages:

-   -   a) The overall waste destruction rate will be increased if the        reaction kinetics of anodically oxidizing mediator “A”,        oxidizing mediator “B” and oxidized mediator “B” oxidizing the        biological waste is sufficiently rapid such that the combined        speed of the three step reaction train is faster than the two        step reaction trains of anodically oxidizing mediator “A” or        “B”, and the oxidized mediators “A” or “B” oxidizing the        biological waste, respectively.    -   b) If the cost of mediator “B” is sufficiently less than that of        mediator “A”, the used of the above three step reaction train        will result in lowering the cost of waste destruction due to the        reduced cost associated with the smaller required inventory and        process losses of the more expensive mediator “A”. An example of        this the use of a silver (II)-peroxysulfate mediator system to        reduce the cost associated with silver and overcome the slow        oxidation kinetics of peroxysulfate only MEO process.    -   c) The MEO process is “desensitized” to changes in the types of        molecular bonds present in the biological waste as the use of        multiple mediators, each selectively attacking different types        of chemical bonds, results in a highly “nonselective” oxidizing        system.        Anolyte Additional Features

In one preferred embodiment of the MEO process in this invention, thereare one or more simple anion redox couple mediators in the anolyteaqueous solution. In a preferred embodiment of the MEO process, thereare one or more complex anion (i.e., POMs) redox couple mediators in theanolyte aqueous solution. In another preferred embodiment of the MEOprocess, there are one or more simple anion redox couples and one ormore complex anion redox couples in the anolyte aqueous solution.

In the MEO process of the invention, anion redox couple mediators in theanolyte part of an aqueous electrolyte solution will use an acid,neutral or alkaline solution depending on the temperature and solubilityof the specific mediator(s).

Some redox couples having an oxidation potential at least equal to thatof the Ce⁺³/Ce⁺⁴ redox couple (i.e., 1.7 volts), and sometimes requiringheating to above about 50° C. (i.e., but less then the boiling point ofthe electrolyte) can initiate a second oxidation process wherein themediator ions in their oxidized form interact with the aqueous anolyte,creating secondary oxidizer free radicals (e.g., •O₂H, •OH, •SO₄, •NO₃,etc.) or hydrogen peroxide. Such mediator species in this invention areclassified herein as “super oxidizers” (SO) to distinguish them from the“basic oxidizers” incapable of initiating this second oxidation process.

The oxidizer species addressed in this patent (i.e., characteristicelements having atomic number below 90) are described in Table I (simpleanions redox couple mediators): Type I IPAs formed by Mo, W, V, Nb, Ta,or mixtures there of as addenda atoms; Type I HPAs formed byincorporation into the aforementioned IPAs if any of the elements listedin Table II (heteroatoms) either singly or in combinations thereof; orany HPA containing at least one heteroatom type (i.e., element)contained in both Table I and Table II; or mediator species from any orall of these generic groups.

Each oxidizer anion element has normal valence states (NVS) (i.e.,reduced form of redox couple) and higher valence states (HVS) (i.e.,oxidized form of redox couple) created by stripping electrons off NVSspecies when they pass through and electrochemical cell. The MEO processof the present invention uses a broad spectrum of anion oxidizers; theseanion oxidizers used in the basic MEO process may be interchanged in thepreferred embodiment without changing the equipment.

In preferred embodiments of the MEO process, the basic MEO process ismodified by the introduction of additives such as tellurate or periodateions which serve to overcome the short lifetime of the oxidized form ofsome redox couples (e.g., Cu⁺³) in the anolyte via the formation of morestable complexes (e.g., [Cu(O₆)₂]⁻⁷, [Cu(HteO₆)₂]⁻⁷). The tellurate andperiodate ions can also participate directly in the MEO process as theyare the oxidized forms of simple anion redox couple mediators (see TableI) and will participate in the oxidation of biological waste in the samemanner as previously described for this class of oxidizing agents.

Alkaline Electrolytes

In one preferred embodiment, a cost reduction will be achieved in thebasic MEO process by using an alkaline electrolyte, such as but notlimited to aqueous solutions of NaOH or KOH with mediator specieswherein the reduced form of said mediator redox couple displayssufficient solubility in said electrolyte to allow the desired oxidationof the infectious waste to proceed at a practical rate. The oxidationpotential of redox reactions producing hydrogen ions (i.e., bothmediator species and infectious waste molecules reactions) are inverselyproportional to the electrolyte pH, thus with the proper selection of aredox couple mediator, it is possible, by increasing the electrolyte pH,to minimize the electric potential required to affect the desiredoxidation process, thereby reducing the electric power consumed per unitmass of infectious waste destroyed.

When an alkaline anolyte (e.g., NaOH, KOH, etc.) is used, benefits arederived from the saponification (i.e., base promoted ester hydrolysis)of fatty acids to form water soluble alkali metal salts of the fattyacids (i.e., soaps) and glycerin, a process similar to the production ofsoap from animal fat by introducing it into a hot aqueous lye solution.

In this invention, when an alkaline anolyte is used, the CO₂ resultingfrom oxidation of the infectious waste reacts with the anolyte to formalkali metal bicarbonates/carbonates. The bicarbonate/carbonate ionscirculate within the anolyte where they are reversibly oxidized topercarbonate ions either by anodic oxidation within the electrochemicalcell or alternately by reacting with the oxidized form of a morepowerful redox couple mediator, when present in the anolyte. Thecarbonate thus functions exactly as a simple anion redox couplemediator, thereby producing an oxidizing species from the infectiouswaste oxidation products that it is capable of destroying additionalinfectious waste.

Additional MEO Electrolyte Features

In one preferred embodiment of this invention, the catholyte and anolyteare discrete entities separated by a membrane, thus they are notconstrained to share any common properties such as electrolyteconcentration, composition, or pH (i.e., acid, alkali, or neutral). Theprocess operates over the temperature range from approximately 0° C. tooslightly below the boiling point of the electrolyte used during thedestruction of Sharps I and biological remaining waste and thesterilization of Sharps II.

MEO Process Augmented by Ultraviolet/Ultrasonic Energy

Decomposition of the hydrogen peroxide into free hydroxyl radicals iswell known to be promoted by ultraviolet (UV) irradiation. Thedestruction rate of biological waste obtained using the MEO process inthis invention, will, therefore, be increased by UV irradiation of thereaction chamber anolyte to promote formation of additional hydroxylfree radicals. In a preferred embodiment, UV radiation is introducedinto the anolyte chamber using a UV source either internal to oradjacent to the anolyte chamber. The UV irradiation decomposes hydrogenperoxide, which is produced by secondary oxidizers generated by theoxidized form of the mediator redox couple, into hydroxyl free radical.The result is an increase in the efficiency of the MEO process since theenergy expended in hydrogen peroxide generation is recovered through theoxidation of biological materials in the anolyte chamber.

Additionally, ultrasonic energy is introduced into the anolyte chamber.Implosion of the microscopic bubbles formed by the rapidly oscillatingpressure waves emanating from the sonic horn generate shock wavescapable of producing extremely short lived and localized conditions of4800° C. and 1000 atmospheres pressure within the anolyte. Under theseconditions water molecules decompose into hydrogen atoms and hydroxylradicals. Upon quenching of the localized thermal spike, the hydroxylradicals will undergo the aforementioned reactions with the Sharps I andII and the biological waste or combine with each other to form anotherhydrogen peroxide which will then itself oxidize additional remainingwaste.

In another preferred embodiment, the destruction rate of non anolytesoluble remaining waste is enhanced by affecting a reduction in thedimensions of the individual second (i.e., biological waste) phaseentities present in the anolyte, thereby increasing the total wastesurface area wetted by the anolyte and therefore the amount of wasteoxidized per unit time. Immiscible liquids may be dispersed on anextremely fine scale within the aqueous anolyte by the introduction ofsuitable surfactants or emulsifying agents. Vigorous mechanical mixingsuch as with a colloid mill or the microscopic scale mixing affected bythe aforementioned ultrasonic energy induced microscopic bubbleimplosion could also be used to affect the desired reduction in size ofthe individual second phase waste volumes dispersed in the anolyte. Thevast majority of tissue based waste will be converted from a semi-rigidsolid into a liquid phase, thus becoming treatable as above, using avariety of cell disruption methodologies. An examples of this method ismechanical shearing using ultrasonic devices (i.e., sonicators) wherethe aforementioned implosion generated shock wave, augmented by the4800° C. temperature spike, shear the cell walls. Distributing the cellprotoplasm throughout the anolyte produces an immediate reduction in themass and volume of actual wastes as about 67 percent of protoplasm isordinary water, which simply becomes part of the aqueous anolyte,requiring no further treatment. If the amount of water released directlyfrom the remaining waste and/or formed as a reaction product from theoxidation of hydrogenous waste dilutes the anolyte to an unacceptablelevel, the anolyte can easily be reconstituted by simply raising thetemperature and/or lowering the pressure in an optional evaporationchamber to affect removal of the required amount of water. The solubleconstituents of the protoplasm are rapidly dispersed throughout theanolyte on a molecular scale while the insoluble constituents will bedispersed throughout the anolyte as an extremely fine second phase usingany of the aforementioned dispersal methodologies, thereby vastlyincreasing the waste anolyte interfacial contact area beyond thatpossible with an intact cell configuration and thus the rate at whichthe remaining waste is destroyed and the MEO efficiency.

MEO Process Augmented with Free Radicals

The principals of the oxidation process used in this invention in whicha free radical (e.g., •O₂H, •OH, •SO₄, •NO₃,) cleaves and oxidizehalogenated hydrocarbon compounds resulting in the formation ofsuccessively smaller hydrocarbon compounds. The intermediate compoundsso formed are easily oxidized to carbon dioxide and water duringsequential reactions.

Inorganic radicals are generated in aqueous solution variants of the MEOprocess in this invention. Radicals have been derived from carbonate,azide, nitrite, nitrate, phosphate, phosphite, sulphite, sulphate,selenite, thiocyanate, chloride, bromide, iodide and formate ions. TheMEO process may generate organic free radicals, such as sulfhydryl. Whenthe MEO process in this invention is applied to halogenated hydrocarbonmaterials they are broken down into organic compounds that are attackedby the aforementioned inorganic free radicals, producing organic freeradicals, which contribute to the oxidation process and increase theefficiency of the MEO process.

SUMMARY

These and further and other objects and features of the invention areapparent in the disclosure, which includes the above and ongoing writtenspecification, with the claims and drawings.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1A MEO Apparatus Diagram is a schematic representation of a systemfor destroying sharps and/or sterilizing sharps. FIG. 1A is arepresentation of a general embodiment of the present invention (withthe understanding that not all of the components shown therein mustnecessarily be employed in all situations and others may be added asneeded for a particular application).

FIG. 1B Anolyte Reaction Chamber for Sharps I (Destruction) is aschematic representation of the anolyte reaction chamber used fordestruction of sharps (normally this anolyte reaction chamber is notused to clean glass and PFTE). This chamber accommodates a continuousfeed of these materials into the chamber. The destruction is normallycomplete however this chamber can be used for the partial destructionwhere the sharps are no longer usable for their intended use.

FIG. 1C Anolyte Reaction Chamber for Sharps II(Sterilization/Disinfection) is a schematic representation of theanolyte reaction chamber used to sterilize glass and PTFE sharps, andmixtures that include large particulate of waste adhering to thesesharps.

FIG. 1D Anolyte Reaction Chamber Remote is a schematic representation ofthe anolyte reaction chamber used for separating the anolyte reactionchamber from the basic MEO apparatus. This configuration allows thechamber to be a part of a primary room, such as an operatorium,laboratory or similar use, minimizing the exposure of the operatingtechnician to the activities in the primary room.

FIG. 1E Anolyte Reaction Chamber—Sharps Repository is a schematicrepresentation of a sharps repository container serving the role of theanolyte reaction chamber that is not a part of the MEO apparatus. Thehospital or similar facilities are required to store sharps in safecontainers until their disposal. This figure depicts the modification ofthese temporary storage containers to replace them with anolyte reactionchambers 5(e) with disconnect joints. The anolyte reaction chamber 5 eis connected to the MEO apparatus and the contents are destroyed. Thecontainer is then returned to use in the facility as a temporary storagecontainer.

FIG. 2 MEO System Model 5.b for Destruction of Sharps is a schematicrepresentation of a typical preferred embodiment. The Model 5.b uses theanolyte reaction chamber 5 a in the MEO apparatus depicted in FIG. 1A.This model is used for the destruction of Sharps I.

FIG. 3 MEO Controller for System Model 5.b is a schematic representationof the MEO electrical and electronic systems. FIG. 2 is a representationof a general embodiment of a controller for the present invention shownin FIG. 2 (with the understanding that not all of the components showntherein must necessarily be employed in all situations and others may beadded as needed for a particular application).

FIG. 4 MEO Model 5.b Operational Steps is a schematic representation ofthe generalized steps of the process used in the MEO apparatus shown inFIG. 2 (with the understanding that not all of the components showntherein must necessarily be employed in all situations and others may beadded as needed for a particular application).

DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS

According to this present patent, the Mediated Electrochemical Oxidation(MEO) process and apparatus may be used for the destruction and/orsterilization of sharps that have been used in animal or human patientcare or treatment or in medical, research, or industrial laboratories.In this patent there is a distinction between the sharps that can bedestroyed and those that can be sterilized. The MEO process andapparatus will decompose the Sharps I into metallic ions in solution inthe anolyte. The MEO process will oxidize the infectious materials onSharps II until they are decomposed into carbon dioxide and water.

MEO Chemistry

Mediated Electrochemical Oxidation (MEO) process chemistry described inthis patent uses oxidizer species (i.e., characteristic elements havingatomic number below 90) as described in Table I (simple anions redoxcouple mediators); Type I IPAs formed by Mo, W, V, Nb, Ta, or mixturesthere of as addenda atoms; Type I HPAs formed by incorporation into theaforementioned IPAs of any of the elements listed in Table II(heteroatoms) either singly or in combination there of; or any HPAcontaining at least one heteroatom type (i.e., element) contained inboth Table I and Table II; or combinations of mediator species from anyor all of these generic groups. Since the anolyte and catholyte arecompletely separated entities, it is not necessary for both systems tocontain the same electrolyte. Each electrolyte may, independent of theother, consist of an aqueous solution of acids, typically but notlimited to nitric, sulfuric, of phosphoric; alkali, typically but notlimited to sodium or potassium hydroxide; or neutral salt typically butnot limited to sodium or potassium salts of the aforementioned strongmineral acids.

The MEO Apparatus is unique in that it accommodates the numerous choicesof mediator ions and electrolytes by simply draining, flushing, andrefilling the system with the mediator/electrolyte system of choice.

Because of redundancy and similarity in the description of the variousmediator ions, only the bromate and nitric acid combination is discussedin detail. However, it is to be understood that the following discussionof the bromate/ perbromate, ((BrO₃ ⁻¹)/(BrO₄ ⁻¹)) redox couple reactionin nitric acid (HNO₃) also applies to all the aforementioned oxidizerspecies and electrolytes described at the beginning of this section.Furthermore, the following discussions of the interaction of perbromateions with aqueous electrolytes to produce the aforementioned freeradicals also applies to all aforementioned mediators having anoxidation potential sufficient to be classified super oxidizers,typically at least equal to that of the Ce⁺³/Ce⁺⁴ redox couple (i.e.,1.7 volts).

FIG. 1A shows a MEO Apparatus in a schematic representation fordestroying of sharps and/or biological remaining waste. At the anode ofthe electrochemical cell 25 Br(V) ions (Br⁺⁵, bromate) are oxidized toBr(VI) ions (BrO₄ ⁻¹, perbromate),BrO₃ ⁻¹+H₂O→BrO₄ ⁻¹+2H⁺+2e⁻

If the anolyte temperature is sufficiently high, typically above 50° C.,the Br(VI) species may undergo a redox reaction with the water in theaqueous anolyte. The oxidation of water proceeds by a sequence ofreactions producing a variety of intermediate reaction products, some ofwhich react with each other. A few of these intermediate reactionproducts are highly reactive free radicals including, but not limited tothe hydroxyl (•OH) and hydrogen peroxy or perhydroxyl (•HO₂) radicals.Additionally, the mediated oxidizer species ions may interact withanions present in the acid or neutral salt electrolyte (e.g., •NO₃ ⁻,•SO₄ ⁻², or •PO₄ ⁻³, etc.) to produce free radicals typified by, but notlimited to •NO₃, or the anions may undergo direct oxidation at the anodeof the cell. The population of hydroxyl free radicals may be increasedby ultraviolet irradiation of the anolyte (see ultraviolet source 11) inthe reaction chamber(s) 5(a,b,c,d) to cleave the hydrogen peroxidemolecules, intermediate reaction products, into two such radicals. Freeradical populations will also be increased by ultrasonic vibration (seeultrasonic source 9) induced by the aforementioned implosion generatedshock wave, augmented by the 4800° C temperature spike and 1000atmospheres pressure.

These secondary oxidation species are capable of oxidizing the Sharps Iand sterilizing Sharps II and thus act in consort with Br(VI) ions inthe MEO process.

The oxidizers react with the Sharps I to oxidize them into metal ions insolution and to oxidize the biological waste adhering to the sharps toproduce CO₂ and water. These processes occur in the anolyte on the anodeside of the system in the reaction chamber(s) 5(a,b,c,d).

Addition of perbromate ions to non-bromate-based MEO systems are alsoproposed as this has the potential for increasing the overall rate ofbiological waste oxidation compared to the non-bromate MEO system alone.(Again it is to be understood this discussion of the bromate/perbromateredox couple also applies to all the aforementioned oxidizer speciesdescribed at the beginning of this section.) If the two step process ofelectrochemically forming the BrO₄ ⁻¹ ion and the BrO₄ ⁻¹ ion oxidizingthe mediator ion to its higher valance occurs faster than the directelectrochemical oxidation of the mediator ion itself, then there is anoverall increase in the rate of destruction of Sharps I and thesterilization of Sharps III.

Membrane 27 separates the anode and the cathode chambers in theelectrochemical cell 25. Hydrogen ions (H⁺) or hydronium ions(H₃O⁺)travel through the membrane 27 due to the electrical potentialfrom the dc power supply 29 applied between the anode(s) and cathodes(s)26 and 28, respectively. In the catholyte the nitric acid is reduced tonitrous acid3HNO₃+6H⁺+6e⁻→3HNO₂+H₂Oby the reaction between the H⁺ ions and the nitric acid. Oxygen isintroduced into the catholyte through the air sparge 37 located belowthe liquid surface, and the nitric acid is regenerated,3HNO₂+3/2O₂→3HNO₃

The overall process results in the destruction of the Sharps I intometallic ions in solution and the biological waste is converted tocarbon dioxide, water, and a small amount of inorganic compounds insolution or as a precipitate, which will be extracted by the inorganiccompound removal and treatment system 15.

The MEO process will operate in three modes (total destruction, partialdestruction, and decontamination). In mode one (total destruction) onethe MEO process will proceed until complete destruction of the Sharps Ihas been complete. In mode two (partial destruction) there is incompletedestruction of Sharps I but there is a significant change in the shapeof the sharp so that it's original use is no longer possible. Theoxidizing species have a tendency to remove the sharp edges and pointsfirst in the oxidizing process. Needles would no longer look like a partof a syringe and scalpels no longer would have sharp cutting edges. Inmode three (decontamination) the MEO process destroys all the infectiouswaste on the Sharps II resulting in sterilized Sharps II but they arenot destroyed because the MEO process does not oxidize them.

The MEO process has been tested using a whole small animal (dead) mouse.After the MEO process had run for a suitable time the physical structureof the mouse was totally converted into a liquid. The liquid was testedand only a very small amount of total carbon content was detected. Thecarbon content of the largest detected hydrocarbon molecules was lessthen thirty (30) carbons per molecule. This result supports theconclusion that the contents of the liquid were sterilized and/ordisinfected. The microorganism tests to determine the existence ofmicroorganism will be completed following accepted protocols tosubstantiate the conclusion that the MEO process sterilizes and/ordisinfects Sharps I and II.

Referring to FIG. 1B, the Sharps I are destroyed (mode one) in thisanolyte reaction chamber. Hinged lid 1 is lifted, the Sharps I areintroduced into the top of sharps basket 3 (the basket is made of PTFE)in the reaction chamber 5 a where the Sharps I remains. The apparatuscontinuously circulates the anolyte portion of the electrolyte directlyfrom the electrochemical cell 25 through the reaction chamber 5 a tomaximize the concentration of oxidizing species contacting the Sharps I.An in-line filter 6 prevents solid particles large enough to clog theelectrochemical cell 25 flow paths from exiting the reaction chamber 5a. Contact of the oxidizing species with incomplete oxidation productsthat are gaseous at the conditions within the reaction chamber 5 a maybe enhanced by using conventional techniques for promoting gas/liquidcontact (e.g., ultrasonic vibration 9, mechanical mixing 7). Allsurfaces of the apparatus in contact with the anolyte or catholyte arecomposed of glass, or nonreactive polymers (e.g., PTFE, PTFE linedtubing, etc.

The anolyte circulation system contains a pump 19 and a removal andtreatment system 15 (e.g., filter, centrifuge, hydrocyclone, etc,) toremove any insoluble inorganic compounds that form as a result ofmediator or electrolyte ions reacting with anions of or containinghalogens, sulfur, phosphorous, nitrogen, etc. that may be present in thewaste stream thus preventing formation of unstable oxycompounds (e.g.,perchlorates, etc.). The anolyte is returned to the electrochemical cell25, where the oxidizing species are regenerated, which completes thecirculation in the anolyte system (A).

Sharps I may be added to the basket 3 in the reaction chamber eithercontinuously or in the batch mode. The anolyte starts either at theoperating temperature or at a lower temperature, which subsequently isincreased by the thermal control 21 to the desired operating temperaturefor the specific anolyte stream. Sharps I may also be introduced intothe apparatus, with the concentration of electrochemically generatedoxidizing species in the anolyte being limited to some predeterminedvalue between zero and the maximum desired operating concentration forthe anolyte stream by control of the electric current by the system dcpower supply 29 supplied to the electrochemical cell 25. The electrolyteis composed of an aqueous solution of mediator species and electrolytesappropriate for the species selected and is operated within thetemperature range from approximately 0° C. to slightly below the boilingpoint of the electrolytic solution, usually less then 100° C., at atemperature or temperature profile most conducive to the desired SharpsI destruction rate (e.g., most rapid, most economical, etc.). The acid,alkaline, or neutral salt electrolyte used will be determined by theconditions in which the species will exist.

Considerable attention has been paid to halogens especially chlorine andtheir deleterious interactions with silver mediator ions, however thisis of much less concern or importance to this invention for thefollowing two reasons. First, the biological waste considered hereintypically contains relatively small amounts of these halogen elementscompared to the halogenated solvents and nerve agents addressed in thecited patents. Second, the wide range of properties (e.g., oxidationpotential, solubility of compounds, cost, etc.) of the mediator speciesclaimed in this patent allows selection of a single or mixture ofmediators either avoiding formation of insoluble compounds, easilyrecovering the mediator from the precipitated materials, or beingsufficiently inexpensive so as to allow the simple disposal of theinsoluble compounds as waste, while still maintaining the capability tooxidize (i.e., destroy) the biological waste economically.

The residue of the inorganic compounds is flushed out of the treatmentsystem 15 during periodic maintenance if necessary. If warranted, theinsoluble inorganic compounds are converted to water-soluble compoundsusing any one of several chemical or electrochemical processes.

The waste destruction process will be monitored by severalelectrochemical and physical methods. Various cell voltages (e.g., opencircuit, anode vs. reference electrode, ion specific electrode, etc.)yield information about the ratio of oxidized to reduced mediator ionconcentrations which will be correlated with the amount of reducingagent (i.e., biological waste) either dissolved in or wetted by theanolyte. If a color change accompanies the transition of the mediatorspecies between it's oxidized and reduced states (e.g., heteropolyblues, etc.), the rate of decay of the color associated with theoxidized state, under zero current conditions, could be used as a grossindication of the amount of reducing agent (i.e., oxidizable waste)present. If no color change occurs in the mediator, it may be possibleto select another mediator to simply serve as the oxidization potentialequivalent of a pH indicator. Such an indicator will be required to havean oxidation potential between that of the working mediator and thebiological species, and a color change associated with the oxidizationstate transition.

The anode reaction chamber off-gas will consist of CO₂ and CO fromcomplete and incomplete combustion (i.e., oxidation) of the carbonaceousmaterial in the biological waste, and possibly oxygen from oxidation ofwater molecules at the anode. Standard anesthesiology practice requiresthese three gases to be routinely monitored in real time under operatingroom conditions, while many other respiratory related medical practicesalso require real time monitoring of these gases. Thus a mature industryexist for the production of miniaturized gas monitors directlyapplicable to the continuous quantitative monitoring of anolyte off-gasfor the presence of combustion products. Although usually not asaccurate and requiring larger samples, monitors for these same gassesare used in the furnace and boiler service industry for flue gasanalysis.

The entireties of U.S. Pat. Nos. 4,686,019; 4,749,519; 4,874,485;4,925,643; 5,364,508; 5,516,972; 5,745,835; 5,756,874; 5,810,995;5,855,763; 5,911,868; 5,919,350; 5,952,542; and 6,096,283 are includedherein by reference for their relevant teachings.

MEO Apparatus

A schematic drawing of the MEO apparatus shown in FIG. 1A MEO ApparatusDiagram illustrates the application of the MEO process to thedestruction of Sharps I and the sterilization of Sharps II anybiological waste remaining. The MEO process will operate in three modes(destruction, sterilization, and decontamination). A schematic drawingof the MEO apparatus shown in FIG. 1A MEO Apparatus Diagram illustratesthe application of the MEO process to Sharps I and II. The MEO apparatusis composed of two separate closed-loop systems containing anelectrolyte solution composed of anolyte and catholyte solutions. Theanolyte and catholyte solutions are contained in the anolyte (A) systemand the catholyte (B) system, respectively. These two systems arediscussed in detail in the following paragraphs. There are numerousvariations on the configuration of the anolyte reaction chamber(s)5(a,b,c,d) and the modes of operation. The anolyte reaction chamber hasnumerous configurations as represented by FIGS. 1B thru 1E. Theconfiguration in FIG. 1B being used in mode one (destruction) will bediscussed as illustrative of the many anolyte reaction chambers andoperation modes combinations. This combination will be discussed indetail in the following paragraphs.

ANOLYTE SYSTEM (A)

The bulk of the anolyte resides in the anolyte reaction chamber 5 ashown in FIG. 1B. The hinged lid I is raised and the Sharps I are placedin the solid waste basket 3 in the reaction chamber 5 a. The anolyteportion of the electrolyte solution contains for example BrO₃ ⁻¹/BrO₄ ⁻¹redox couple anions and secondary oxidizing species (e.g., freeradicals, •H₂O₂, etc.). The bulk of the anolyte resides in the anolytereaction chamber 5 a. The anolyte is circulated into the reactionchamber 5 a through the electrochemical cell 25 by pump 19 on the anode26 side of the membrane 27. A membrane 27 in the electrochemical cell 25separates the anolyte portion and catholyte portion of the electrolyte.A filter 6 is located at the base of the reaction chamber 5 a to limitthe size of the solid particles to approximately 1 mm in diameter (i.e.,smaller than the minimum dimension of the anolyte flow path in theelectrochemical cell 25). Small thermal control units 21 and 22 areconnected to the flow stream to heat or cool the anolyte to the selectedtemperature range. The heat exchanger 23 lowers the temperature of theanolyte entering the electrochemical cell and the heat exchanger 24raises the temperature before it enters the anolyte reaction chamber 5a. The electrochemical cell 25 is energized by a DC power supply 29,which is powered by the AC power supply 30. The DC power supply 29 islow voltage high current supply usually operating below 10V DC but notlimited to that range. The AC power supply 30 operates off a typical110v AC line for the smaller units and 240v AC for the larger units.

The oxidizer species population produced by electrochemical generation(i.e., anodic oxidation) of the oxidized form of the redox couplesreferenced herein can be enhanced by conducting the process at lowtemperatures, thereby reducing the rate at which thermally activatedparasitic reactions consume the oxidizer. If warranted a heat exchanger23 can be located immediately upstream from the electrochemical cell 25to lower the anolyte temperature within the cell to the desired level.Another heat exchanger 24 can be located immediately upstream of theanolyte reaction chamber inlet to control the anolyte temperature in thereaction chamber to within the desired temperature range to affect thedesired chemical reactions at the desired rates.

The electrolyte containment boundary is composed of materials resistantto the oxidizing electrolyte (e.g., PTFE, PTFE lined tubing, glass,etc.). Reaction products resulting from the oxidizing processesoccurring in the anolyte system (A) of the system that are gaseous atthe anolyte operating temperature and pressure are discharged to thecondenser 13. The more easily condensed products of incomplete oxidationare separated in the condenser 13 from the anolyte off-gas stream andare returned to the anolyte reaction chamber 5 a for further oxidation.The non-condensable incomplete oxidation products (e.g., low molecularweight organics, carbon monoxide, etc.) are reduced to acceptable levelsfor atmospheric release by a gas cleaning system 16. The gas cleaningsystem 16 is not a necessary component of the MEO apparatus for thedestruction of most types of Sharps I.

If the gas cleaning system 16 is incorporated into the MEO apparatus,the anolyte off-gas is contacted in a counter current flow gas scrubbingsystem in the off-gas cleaning system 16 wherein the noncondensiblesfrom the condenser 13 are introduced into the lower portion of thecolumn through a flow distribution system of the gas cleaning system 16and a small side stream of freshly oxidized anolyte direct from theelectrochemical cell 25 is introduced into the upper portion of thecolumn. This will result in the gas phase continuously reacting with theoxidizing mediator species as it rises up the column past the downflowing anolyte. Under these conditions the gas about to exit the top ofthe column will have the lowest concentration of oxidizable species andwill also be in contact with the anolyte having the highestconcentration of oxidizer species thereby promoting reduction of any airpollutants present down to levels acceptable for release to theatmosphere. Gas-liquid contact within the column will be promoted by anumber of well established methods (e.g., packed column, pulsed flow,ultrasonic mixing, etc,) that will not result in any meaningful backpressure within the anolyte flow system.

The major products of the oxidation of the biological waste are CO₂, andwater (including minor amounts of CO and inorganic salts), where the CO₂is vented 14 out of the system.

An optional inorganic compound removal and treatment systems 15 is usedshould there be more than trace amount of halogens, or other precipitateforming anions present in the biological waste being processed, therebyprecluding formation of unstable oxycompounds (e.g., perchlorates,etc.).

The MEO process will proceed until complete destruction of the Sharps Ihas been affected or be modified to stop the process at a point wherethe destruction of the Sharps I are incomplete. The reason for stoppingthe process is that the biological waste materials are benign and do notneed further treatment. The organic compounds recovery system 17 is usedto perform this process.

CATHOLYTE SYSTEM (B)

The bulk of the catholyte is resident in the catholyte reaction chamber31. The catholyte portion of the electrolyte is circulated by pump 43through the electrochemical cell 25 on the cathode 28 side of themembrane 27. The catholyte portion of the electrolyte flows into acatholyte reservoir 31. Small thermal control units 45 and 46 areconnected to the catholyte flow stream to heat or cool the catholyte tothe selected temperature range. External air is introduced through anair sparge 37 into the catholyte reservoir 31. The oxygen contained inthe air oxidizes nitrous acid and the small amounts of nitrogen oxides(NO_(x)), produced by the cathode reactions, to nitric acid and NO₂,respectively. Contact of the oxidizing gas with nitrous acid may beenhanced by using conventional techniques for promoting gas/liquidcontact by a mixer 35 (e.g., ultrasonic vibration 48, mechanical mixing35, etc.). Systems using non-nitric acid catholytes may also require airsparging to dilute and remove off-gas such as hydrogen. An off-gascleaning system 39 is used to remove any unwanted gas products (e.g.NO₂, etc.). The cleaned gas stream, combined with the unreactedcomponents of the air introduced into the system is discharged throughthe atmospheric vent 47.

Optional anolyte recovery system 41 is positioned on the catholyte side.Some mediator oxidizer ions may cross the membrane 27 and this option isavailable if it is necessary to remove them through the anolyte recoverysystem 41 to maintain process efficiency or cell operability, or theireconomic worth necessitates their recovery. Operating theelectrochemical cell 25 at higher than normal membrane 27 currentdensities (i.e., above about 0.5 amps/cm²) will increase the destructionrate of biological waste and Sharps I, but also result in increasedmediator ion transport through the membrane into the catholyte. It maybe economically advantageous for the electrochemical cell 25 to beoperated in this mode. It is advantageous whenever the replacement costof the mediator species or removal/recovery costs are less than the costbenefits of increasing the Sharps I throughput (i.e., oxidation rate) ofthe electrochemical cell 25. Increasing the capitol cost of expandingthe size of the electrochemical cell 25 can be avoided by using thisoperational option.

SYSTEM MODEL

A preferred embodiment, MEO System Model 5.b (shown in FIG. 2 MEO SystemModel 5.b) is sized for use in a hospital ward or medical laboratory.Other preferred embodiments have differences in the externalconfiguration and size but are essentially the same in internal functionand components as depicted in FIGS. 1A. The preferred embodiment in FIG.2 comprises a housing 72 constructed of metal or high strength plasticsurrounding the electrochemical cell 25, the electrolyte and theforaminous basket 3. The AC power is provided to the AC power supply 30by the power cord 78. A monitor screen 51 is incorporated into thehousing 72 for displaying information about the system and about theSharps I and biological waste being treated. Additionally, a controlkeyboard 53 is incorporated into the housing 72 for inputtinginformation into the system. The monitor screen 51 and the controlkeyboard 53 may be attached to the system without incorporating theminto the housing 72. In a preferred embodiment, status lights 73 areincorporated into the housing 72 for displaying information about thestatus of the treatment of the Sharps I and biological waste material.An air sparge 37 is incorporated into the housing 72 to allow air to beintroduced into the catholyte reaction chamber 31 below the surface ofthe catholyte. In addition, a CO₂ vent 14 is incorporated into thehousing 72 to allow for CO₂ release from the anolyte reaction chamberhoused within. In a preferred embodiment, the housing includes means forcleaning out the MEO waste treatment system, including a flush(s) 18 anddrain(s) 12 through which the anolyte and catholyte will pass. Thepreferred embodiment further comprises an atmospheric vent 47facilitating the releases of gases into the atmosphere from thecatholyte reaction chamber 31. Other preferred embodiment systems aresimilar in nature but are scaled up in size to handle a larger capacityof waste, such as hospital wing, operating rooms, laboratories,incinerator replacement units, etc.

The system has a control keyboard 53 for input of commands and data. TheOn/Off button 74 is used to turn the apparatus power on and off. Thereis a monitor screen 51 to display the systems operation and functions.Below the keyboard 53 and monitor screen 51 are the status lights 73 foron, off, and standby. Hinged lid 1 is opened and the Sharps I aredeposited in the basket 3 in the chamber 5 a. A lid stop 2 keeps the lidopening controlled. The hinged lid 1 is equipped with a locking latch 76that is operated by the controller 49. In the chamber 5 a is the aqueousacid, alkali, or neutral salt electrolyte and mediated oxidizer speciessolution in which the oxidizer form of the mediator redox coupleinitially may be present or may be generated electrochemically afterintroduction of the Sharps I and application of DC power 30 to theelectrochemical cell 25. Similarly, the sharps will be introduced whenthe anolyte is at room temperature, operating temperature or someoptimum intermediate temperature. DC power supply 30 provides directcurrent to an electrochemical cell 25. Pump 19 circulates the anolyteportion of the electrolyte and the Sharps I and biological wastematerial is rapidly oxidized at temperatures below 100° C. and ambientpressure. An in-line filter 6 prevents solid particles large enough toclog the electrochemical cell 25, flow paths from exiting this reactionchamber 5 a. The oxidation process will continue to break the Sharps Iand biological waste materials down into smaller and smaller moleculesuntil they reach metallic ions in solution and the biological materialsinto CO₂, water, and some CO and inorganic salts. Any residue ispacified in the form of a salt and may be periodically removed throughthe Inorganic Compound Removal and Treatment System 15 and drain outlets12. The electrolyte can be replaced with a different electrolyte whenusing the same plumbing for their introduction into the reactionchambers 5 a and 31 changes the application or materials to bedestroyed. The catholyte reservoir 31 has a screwed top 33 (shown inFIG. 1A), which allow access to the reservoir 31 for cleaning andmaintenance by service personnel.

The MEO apparatus as an option may be placed in a standby mode withSharps I and biological waste being added as it is generated throughoutthe day and the unit placed in full activation during non-businesshours. The MEO process advantageous properties of low power consumptionand very low loses of the mediated oxidizer species and electrolyte,provide as an option for the device to be operated at a low level duringthe day to achieve a slow rate of destruction of Sharps I and thebiological waste throughout the day.

The compactness of the device makes it ideal for offices and operatingrooms as well as being suitable for use with high volume inputs oflaboratories and hospitals non-operating room activities. The processoperates at low temperature and ambient atmospheric pressure and doesnot generate toxic compounds during the destruction of Sharps I and ofbiological waste, making the process indoors compatible. The system isscalable to a unit large enough to replace a hospital incinerator systemand remove the requirement of transporting Sharps I to offsitelocations. The CO₂ oxidation product from the anolyte system A is ventedout the CO₂ vent 14. The off-gas products from the catholyte system B isvented through the atmospheric air vent 47 as shown.

SYSTEM CONTROLLER

An operator runs the MEO Apparatus illustrated by FIG. 1A, FIG. 1B andFIG. 2 by using the MEO Controller depicted in FIG. 3 MEO Controller.The controller 49 with microprocessor is connected to a monitor 51 and akeyboard 53. The operator inputs commands to the controller 49 throughthe keyboard 53 responding to the information displayed on the monitor51. The controller 49 runs a program that sequences the steps for theoperation of the MEO apparatus. The program has pre-programmed sequencesof standard operations that the operator will follow or he will choosehis own sequences of operations. The controller 49 will allow theoperator to select his own sequences within limits that assure a safeand reliable operation. The controller 49 sends digital commands thatregulates the electrical power (AC 30 and DC 29) to the variouscomponents in the MEO apparatus; pumps 19 and 43, mixers 7 and 35,thermal controls 21, 22, 45, 46, ultraviolet sources 11, ultrasonicsources 9 and 48, CO₂ vent 14, air sparge 37, and electrochemical cell25. The controller receives component response and status from thecomponents. The controller sends digital commands to the sensors toaccess sensor information through sensor responses. The sensors in theMEO apparatus provide digital information on the state of the variouscomponents. Sensors measure flow rate 59, temperature 61, pH 63, CO₂venting 65 degree of oxidation 67, air sparge sensor 69, etc. Thecontroller 49 receives status information on the electrical potential(voltmeter 57) across the electrochemical cell, or individual cells if amulti-cell configuration, and between the anode(s) and referenceelectrodes internal to the cell(s) 25 and the current (ammeter 55)flowing between the electrodes within each cell.

STEPS OF THE OPERATION OF THE MEO PROCESS (B)

The steps of the operation of the MEO process (as shown in FIGS. 1A, 1Band 2) are depicted in FIG. 4 MEO Model 5.b Operational Steps. This MEOapparatus is contained in the housing 72. The MEO system is started 81by the operator engaging the ‘ON’ button 74 (status lights 73) on thecontrol keyboard 53. The system controller 49, which contains amicroprocessor, runs the program that controls the entire sequence ofoperations 82. The monitor screen 51 displays the steps of the processin the proper sequence. The status lights 73 on the panel provide thestatus of the MEO apparatus (e.g. on, off, ready, standby). The lid 1 isopened and the Sharps I(with the associated biological waste)are placed83 in the basket 3, whereupon the solid portion of the waste is retainedand the liquid portion flows through the basket and into the anolyte.The locking latch 76 is activated. The pumps 19 and 43 begin circulation85 of the anolyte 87 and catholyte 89, respectively. As soon as theelectrolyte circulation is established throughout the system, the mixers7 and 35 begin to operate 91 and 93. Depending upon biological wastecharacteristics (e.g., reaction kinetics, heat of reaction, etc.) it maybe desirable to introduce the Sharps I and biological waste into a roomtemperature or cooler anolyte system with little or none of the mediatorredox couple in the oxidizer form. Once flow is established the thermalcontrols units 21, 22, 45, and 46 are turned on 95/97, initiatingpredetermined anodic oxidation and electrolyte heating programs. Theelectrochemical cell 25 is energized 94 (by cell commands 56) to theelectric potential 57 and current 55 density determined by thecontroller program. By using programmed electrical power and electrolytetemperature ramps it is possible to maintain a predetermined Sharps Idestruction rate profile such as a relatively constant reaction rate asthe more reactive waste components are oxidized, thus resulting in theremaining waste becoming less and less reactive, thereby requiring moreand more vigorous oxidizing conditions. The ultrasonic 9 and 48 andultraviolet systems 11 are activated 99 and 101 in the anolyte reactionchamber 5 a and catholyte reaction chamber 31 if those options arechosen in the controller program. The CO₂ vent 14 is activated 103 torelease CO₂ from the biological waste oxidation processed in the anolytereaction chamber 5 a. The air sparge 37 and atmospheric vent 47 areactivated 105 in the catholyte system. The progress of the destructionprocess will be monitored in the controller (oxidation sensor 67) byvarious cell voltages and currents 55, 57 (e.g., open circuit, anode vs.reference electrode, ion specific electrodes, etc,) as well asmonitoring anolyte off-gas (using the sensor 65) composition for CO₂, COand oxygen content.

The Sharps I are decomposed in to metallic ion in solution. Thebiological waste is being decomposed into water and CO₂ the latter beingdischarged 103 out of the CO₂ vent 14. Air sparge 37 draws air 105 intothe catholyte reservoir 31, and excess air is discharged out theatmospheric vent 47. When the oxidation sensors 65 and 67 determine thedesired degree of waste destruction has been obtained 107, the systemgoes to standby 109. The system operator executes system shutdown 111using the controller keyboard 53.

EXAMPLES

The following examples illustrate the application of the process and theapparatus.

Example 1

Destruction of Biological Specimens:

The MEO apparatus using the MEO process was tested using a number ofwhole small animals (dead mice). The MEO process was run at less then100 watts for approximately an hour. The entire physical structure ofthe mouse was totally converted into a liquid. The liquid was testedusing GC/FID analysis and did not show evidence of any hydrocarbonspresent. The detection limit for this analysis method (GC/FID) isapproximately 1 to 10 ppm (parts per million). This result supports theconclusion that the contents of the liquid were sterilized anddisinfected. The microorganism tests to determine the existence ofmicroorganism will be completed following accepted protocols tosubstantiate the conclusion that the MEO process sterilizes and/ordisinfects Sharps I and II.

Example 2

Efficient and Environmentally Safe Products:

The MEO process produces metallic ions in solution and the biologicalwaste decomposes into CO₂, water, and trace inorganic salts all of whichare considered benign for introduction into the environment byregulatory agencies. The cost of using the MEO process in this inventionis competitive with both the incineration and landfill methodologies.The MEO process is uniquely suited for destruction of biological wastebecause water, which constitutes a major portion of this waste (e.g.,tissue, bodies fluids, etc.) is either benign or actually a source ofsecondary oxidizing species, rather than parasitic reactions competingfor the mediator oxidizing species. Furthermore, the energy that must beprovided in the MEO process to heat the waste stream water componentfrom ambient to the electrolyte operating temperature (i.e., 80° C.maximum temperature increase) is trivial compared to the water enthalpyincrease required in autoclave or incineration based processes.

Example 3

Benign In-door Operation:

The system is unique relative to earlier art, since it is built tooperate in an indoor environment such as a hospital room or laboratorywhere it must be compatible with people working in close proximity tothe system as well as people being treated for medical conditions. Theamount of infectious waste adhering to the sharps is generally verysmall in weight and volume thus the carbon dioxide emitted from thedecomposition is equally small. The system is suitable for indoor use inspaces inhabited by personnel as well as for industrial workspacessimilar to an incinerator building.

Example 4

Inherently Safe Operation:

The system is built to require limited operating skill. The systemcontroller is programmed to guide the operator through the normaloperating cycle as well as the various options available. The system isaccessible during its operating cycle so that additional sharps may beadded to materials in process, while remaining compatible with the roomenvironment. When new sharps are to be added to the system duringoperation the operator selects that option. The system controllerrecycles the system operational steps back to step 83. It deactivatessteps 85, 87, 89, 91, 93, 94, 95, 97, 99, 101 and maintains steps 103and 105 in their active mode. The controller releases the locking latch76 and the operator will add additional sharps. After he has completedthe addition he selects the restart option. The system recycles backthrough these steps to continue the processing of the waste.

Example 5

Chemical Reactions are Safe:

The system is built to operate with materials that are safe to handle inthe environment in which it is to be used. The sharps and biologicalwaste contains little or no substances that react with our choice ofelectrolytes to produce volatile-compounds that will offer a problem inthe room environment. The system will operate at temperatures fromapproximately 0° C. to slightly less then the boiling point of theelectrolyte, which is usually less then 100° C. and at ambientatmospheric pressure, which adds to the indoor compatibility.

Example 6

A Green Machine:

The simplicity of the new system built for use with sharps andbiological waste produces a system more economically to operate andcleaner to use than existing waste treatments. The system complexity isreduced by comparison to previous MEO systems, since there is not arequirement to deal with large quantities of halogens. The system has alarge choice of mediators and electrolytes thus providing options thatavoid the problems created by only having a limited selection ofmediators and electrolytes. The system is truly a ‘green machine’ in thesense of an environmentally benign system.

Example 7

System Flexibility:

The system is built so that the composition of the electrolyte may bechanged to adapt the system to a selected composition of sharps andbiological waste. The system is configured with ports to flush and drainthe anolyte and catholyte separately.

Example 8

System By-Products are Safe:

The system flexibility provides for the introduction of more then onemediator ion resulting in marked improvement in the efficiency of theelectrolyte. Furthermore, it desensitizes the electrolyte to chlorineions in solution (i.e. allows increased ease in preventing formation ofunstable perchlorate compounds).

While the invention has been described with reference to specificembodiments, modifications and variations of the invention may beconstructed without departing from the scope of the invention, which isdefined in the following characteristics and features.

The invention provides the following new characteristics and features:

-   -   1. A process for treating and oxidizing Sharps I and sterilizing        Sharps II and biological waste materials comprising disposing an        electrolyte in an electrochemical cell, separating the        electrolyte into an anolyte portion and a catholyte portion with        an ion-selective membrane or semipermeable membrane applying a        direct current voltage between the anolyte portion and the        catholyte portion, placing the sharps and biological waste in        the anolyte portion, oxidizing the Sharps I into metallic ions        in solution in the anolyte, sterilizing Sharps II, and        biological waste in the anolyte portion with a mediated        electrochemical oxidation (MEO) process, wherein the anolyte        portion further comprises a mediator in aqueous solution and the        electrolyte is an acid, neutral or alkaline aqueous solution.    -   2. The process of paragraph 1, wherein:        -   a. the anolyte portion further comprises one or more simple            anions mediator ions species selected from the group            described in Table I (in the aqueous solution and the            electrolyte is an acid, neutral or alkaline solution;        -   b. The oxidizing species are selected from one or more Type            I isopolyanions (i.e., complex anion redox couple mediators)            containing tungsten, molybdenum, vanadium, niobium,            tantalum, or combinations thereof as addenda atoms in            aqueous solution and the electrolyte is an acid, neutral or            alkaline aqueous solution;        -   c. The oxidizing species are selected from one or more Type            I heteropolyanions formed by incorporation into the            aforementioned isopolyanions, as heteroatoms, any of the            elements listed in Table II, either singly or in combination            thereof in the aqueous solutions and the electrolyte is an            acid, neutral, or alkaline aqueous solution;        -   d. The oxidizing species are selected from one or more of            any heteropolyanions containing at least one heteroatom type            (i.e., element) contained in both Table I and Table II_in            the aqueous solutions_and the_electrolyte is an acid,            neutral, or alkaline aqueous solution;        -   e. The oxidizing species are selected from combinations of            anion redox couple mediators from any or all of the previous            four subparagraphs (2a., 2b., 2c., and 2d.);        -   f. adding stabilizing compounds to the electrolyte such as            tellurate or periodate ions which serve to overcome and            stabilize the short lifetime of the oxidized form of the            higher oxidation state species of the simple and complex            anion redox couple mediators;        -   g. the oxidizing species are elements having atomic numbers            less than 90 and identified in Table I;        -   h. each of the species has normal valence states and higher            valence oxidizing states and further comprising creating the            higher valence oxidizing states of the oxidizing species by            stripping electrons from normal valence state species in the            electrochemical cell;        -   i. the oxidizing species are “super oxidizers” (SO)            typically exhibit oxidation potentials at least equal to            that of the Ce⁺³/Ce⁺⁴ redox couple (i.e., 1.7 volts at 1            molar, 25° C. and pH 1) which are redox couple species that            have the capability of producing free radicals such as            hydroxyl or perhydroxyl and further comprising creating            secondary oxidizers by reacting the SO's with water;        -   j. using an alkaline solution for aiding decomposing of the            infectious waste materials derived from the saponification            (i.e., base promoted ester hydrolysis) of fatty acids to            form water soluble alkali metal salts of the fatty acids            (i.e., soaps) and glycerin, a process similar to the            production of soap from animal fat by introducing it into a            hot aqueous lye solution.;        -   k. using an alkaline anolyte solution that absorbs CO₂            forming from oxidation of the biological waste sodium            bicarbonate/carbonate solution which subsequently circulates            through the electrochemical cell, producing a percarbonate            oxidizer;        -   l. using oxidizing species from the MEO process inorganic            free radicals generated in aqueous solutions from species            such as but not limited to carbonate, azide, nitrite,            nitrate, phosphite, phosphate, sulfite, sulfate, selenite,            thiocyanate, chloride, bromide, iodide, and formate            oxidizing species;        -   m. the regeneration of the oxidizer part of the redox couple            in the anolyte portion is done within the electrochemical            cell;        -   n. the membrane(separator between anolyte and catholyte            solutions) can be microporous plastic, sintered glass frit,            etc.;        -   o. the impression of an AC voltage upon the DC voltage to            retard the formation of cell performance limiting surface            films on the electrode;        -   p. disposing a foraminous basket in the anolyte;        -   q. adding oxygen (this is necessary only for HNO₃ ⁻ or NO₃ ⁻            salts) to the catholyte portion;        -   r. the oxidizer species addressed in this patent are            described in: Table I (simple anions); Type I isopolyanions            containing tungsten, molybdenum, vanadium, niobium,            tantalum, or combinations thereof as addenda atoms; Type I            heteropolyanions formed by incorporation into the            aforementioned isoopolyanions, as heteroatoms, any of the            elements listed in Table II, either singly or in            combinations thereof; or any heteropolyanions containing at            least one heteroatom type (i.e., element) contained in both            Table I and Table II;        -   s. lower the temperature (e.g. between 0° C. and room,            temperature) of the anolyte before it enters the            electrochemical cell to enhance the generation of the            oxidized form of the anion redox couple mediator;        -   t. raise the temperature of the anolyte entering the anolyte            reaction chamber to affect the desired chemical reactions at            the desired rates following the lowering of the temperature            of the anolyte entering the electrochemical cell;        -   u. the evolved oxygen from the anode is feed to a hydrogen            fuel apparatus to increase the percentage oxygen available            from the ambient air.    -   3. The process of paragraph 1, wherein:        -   a. introducing an ultrasonic energy into the anolyte portion            rupturing cell membranes in the biological waste materials            by momentarily raising local temperature within the cell            membranes with the ultrasonic energy to above several            thousand degrees and causing cell membrane failure;        -   b. introducing ultraviolet energy into the anolyte portion            and decomposing hydrogen peroxide and ozone into hydroxyl            free radicals therein, thereby increasing efficiency of the            MEO process by converting products of electron consuming            parasitic reactions (i.e., ozone and hydrogen peroxide) into            viable free radical (i.e., secondary) oxidizers without the            consumption of additional electrons;        -   c. using a surfactant to be added to the anolyte promote            dispersion of the biological waste or intermediate stage            reaction products within the aqueous solution when these            biological waste or reaction products are not water-soluble            and tend to form immiscible layers;        -   d. using simple and/or complex redox couple mediators, and            attacking specific organic molecules with the oxidizing            species while operating at low temperatures thus preventing            the formation of dioxins and furans;        -   f. breaking down biological waste materials into organic            compounds and attacking the organic compounds using either            the simple and/or complex anion redox couple mediator or            inorganic free radicals to generating organic free radicals;        -   g. raising normal valence state anions to a higher valence            state and stripping the normal valence state anions of            electrons in the electrochemical cell; [The oxidized forms            of any other redox couples present are produced either by            similar anodic oxidation or reaction with the oxidized form            of other redox couples present. The oxidized species of the            redox couples oxidize the biological waste molecules and are            themselves converted to their reduced form, whereupon they            are reoxidized by either of the aforementioned mechanisms            and the redox cycle continues]        -   h. circulating anions through an electrochemical cell to            affect the anodic oxidation of the reduced form of the            reversible redox couple into the oxidized form;        -   i. contacting anions with biological waste materials in the            anolyte portion;        -   j. circulating anions through the electrochemical cell;        -   k. involving anions with an oxidation potential above a            threshold value of 1.7 volts (i.e., super oxidizer) in a            secondary oxidation process and producing oxidizers;        -   l. adding a ultra-violet (UV) energy source to the anolyte            portion and augmenting secondary oxidation processes,            breaking down hydrogen peroxide and ozone into hydroxyl free            radicals, and thus increasing the oxidation processes;        -   m. introducing an ultrasonic energy source into the anolyte            portion and irradiating cell membranes in biological waste            materials and momentarily raising local temperature within            the cell membranes and causing cell membrane failure            creating greater exposure of cell contents to oxidizing            species in the anolyte portion; and        -   n. The oxidizer species addressed in this patent (I.e.,            characteristic elements having atomic number below 90) are            described in Table I (simple anions redox couple mediators):            Type I IPAs formed by Mo, W, V, Nb, Ta, or mixtures there            of; Type I HPAs formed by incorporation into the            aforementioned IPAs if any of the elements listed in Table            II (heteroatoms) either singly or in thereof; Or any HPA            containing at least one heteroatom type (i.e., element)            contained in both Table I and Table II or combinations            mediator species from any or all of these generic groups.    -   4. The process of paragraph 1, further comprising:        -   a. using oxidizer species that are found in situ in the            sharps and biological waste to be destroyed, by circulating            the waste-anolyte mixture through an electrochemical cell            where the oxidized form of the in situ reversible redox            couple will be formed by anodic oxidation or alternately            reacting with the oxidized form of a more powerful redox            couple, if added to the anolyte and anodically oxidized in            the electrochemical cell, thereby destroying the biological            waste material;        -   b. using an alkaline electrolyte, such as but not limited to            NaOH or KOH with mediator species wherein the reduced form            of said mediator redox couple displays sufficient solubility            in said electrolyte to allow the desired oxidation of the            biological waste to proceed at a practical rate. The            oxidation potential of redox reactions producing hydrogen            ions (i.e., both mediator species and biological waste            molecules reactions) are inversely proportional to the            electrolyte pH, thus with the proper selection of a mediator            redox couple, it is possible, by increasing the electrolyte            pH, to minimize the electric potential required to affect            the desired oxidation process, thereby reducing the electric            power consumed per unit mass of biological waste destroyed;        -   c. the aqueous solution is chosen from acids such as but not            limited to nitric acid, sulfuric acid, or phosphoric acid,            or mixtures thereof; or alkalines such as but not limited to            of sodium hydroxide or potassium hydroxide, or mixtures            thereof, or neutral electrolytes, such as but not limited to            sodium or potassium nitrates, sulfates, or phosphates or            mixtures thereof; and        -   d. the use of ultrasonic energy induce microscopic bubble            implosion which will be used to affect a desired reduction            in sized of the individual second phase waste volumes            dispersed in the anolyte.    -   5. The process of paragraph 1, further comprising:        -   a. interchanging oxidizing species in a preferred embodiment            without changing equipment; and        -   b. the electrolyte is acid, neutral, or alkaline in aqueous            solution.    -   6. The process of paragraph 1, further comprising:        -   a. the treating and oxidizing Sharps I and sterilizing            Sharps II and biological waste material comprises treating            and oxidizing waste from veterinary industry waste as            identified under the definition of biological waste hereto            referred;        -   b. separating the anolyte portion and the catholyte portion            with a hydrogen or hydronium ion-permeable membrane or            microporous polymer, ceramic or glass frit membrane;        -   c. applying an externally induced electrical potential            induced between the anode(s) and cathode(s) plates of the            electrochemical cell at a electrical potential sufficient to            form the oxidized form of the redox couple having the            highest oxidation potential in the anolyte;        -   d. introducing sharps and biological waste materials into            the anolyte portion;        -   e. forming the reduced form of one or more reversible redox            couples by contacting with oxidizable molecules, the            reaction with which oxidizes the oxidizable material with            the concuminent reduction of the oxidized form of the            reversible redox couples to their reduced form;        -   f. a ultrasonic source connected to the anolyte for            augmenting secondary oxidation processes by momentarily            heating the hydrogen peroxide in the electrolyte to 4800° C.            at 1000 atmospheres thereby dissociating the hydrogen            peroxide into hydroxyl free radicals thus increasing the            oxidation processes;        -   g. oxidation potentials of redox reactions producing            hydrogen ions are inversely related to pH;        -   h. The process of paragraph 1, characterized in that the            process is performed at a temperature from slightly above            0° C. to slightly below the boiling point of the electrolyte            usually less then 100° C.;        -   i. the temperature at which the process is performed is            varied;        -   j. the treating and oxidizing biological waste comprises            treating and oxidizing solid waste;        -   k. the treating and oxidizing biological waste comprises            treating and oxidizing liquid waste;        -   l. the treating and oxidizing biological waste comprises            treating and oxidizing a combination of liquids and solids;            and        -   m. removing and treating precipitates resulting from            combinations of oxidizing species and other species released            from the biological waste during destruction.    -   7. The process of paragraph 1, further comprising that it is not        necessary for both the anolyte and catholyte solutions to        contain the same electrolyte rather each electrolyte system may        be independent of the other, consisting of an aqueous solution        of acids, typically but not limited to nitric, sulfuric or        phosphoric; alkali, typically but not limited to sodium or        potassium hydroxide; or neutral salt, typically but not limited        to sodium or potassium salts of the afore mentioned strong        acids.    -   8. The process of paragraph 1, further comprising the operating        of the electrochemical cell at a current density greater then        0.5 amp per square centimeter across the membrane, even though        this is the limit over which there is the possibility that        metallic anions may leak through the membrane in small        quantities, and recovering the metallic anions through a devise        such as a resin column thus allowing a greater rate of        destruction of materials in the anolyte chamber.    -   9. The process of paragraph 1, wherein:        -   the catholyte solution further comprises an aqueous solution            and the electrolyte in the solution is composed of acids,            typically but not limited to nitric, sulfuric or phosphoric;            or alkali, typically but not limited to sodium or potassium            hydroxide; or neutral salt, typically but not limited to            sodium ornpotassium salts of the afore mentioned strong            acids;        -   a. adding oxygen (this is necessary only for HNO₃ ⁻ or NO₃ ⁻            salts) to the catholyte portion;        -   b. concentration of electrolyte in the catholyte will be            governed by its effect upon the conductivity of the            catholyte solution desired in the electrochemical cell;        -   c. ultrasonic energy induced microscopic bubble implosion            will be used to affect vigorous mixing in the catholyte            solution where it is desirable to oxidize nitric acid and            the small amounts of nitrogen oxides when nitric acid is            used in the catholyte electrolyte;        -   d. mechanical mixing will be used to affect vigorous mixing            in the catholyte solution where it is desirable to oxidize            nitric acid and the small amounts of nitrogen oxides;        -   e. air is introduced into the catholyte solution to promote            oxidation of nitric acid and the small amounts of nitrogen            oxides when nitric acid is used in the catholyte            electrolyte;        -   g. air is introduced into the catholyte solution to dilute            any hydrogen produced in the catholyte solution before being            released; and        -   h. hydrogen gas evolving from the cathode is feed to an            apparatus that uses hydrogen as a fuel such as a proton            exchange membrane (PEM)fuel cell.    -   10. An apparatus for treating and oxidizing Sharps I and        sterilizing sharps II and biological waste materials comprising        an electrochemical cell, an electrolyte disposed in the        electrochemical cell,, a hydrogen or hydronium ion-permeable        membrane, disposed in the electrochemical cell for separating        the cell into anolyte and catholyte chambers and separating the        electrolyte into anolyte and catholyte portions, electrodes        further comprising an anode and a cathode disposed in the        electrochemical cell respectively in the anolyte and catholyte        chambers and in the anolyte and catholyte portions of the        electrolyte, a power supply connected to the anode and the        cathode for applying a direct current voltage between the        anolyte and the catholyte portions of the electrolyte, a        foraminous basket disposed in the anolyte chamber for receiving        the sharps and biological waste materials, oxidizing the sharps        into metallic ions in solution in the anolyte, and oxidizing of        the biological waste materials in the anolyte portion with a        mediated electrochemical oxidation (MEO) process wherein the        anolyte portion further comprises a mediator in aqueous solution        and the electrolyte is an acid, neutral or alkaline aqueous        solution.    -   11. The apparatus of paragraph 10, wherein:        -   a. additives for introducing into the electrolyte and            contributing to kinetics of the mediated electrochemical            processes while keeping it from becoming directly involved            in the oxidizing of the biological waste materials;        -   b. the oxidizer species addressed in this patent (i.e.,            characteristic elements having atomic number below 90) are            described in Table I (simple anions redox couple mediators);        -   c. the oxidizer species addressed in this patent are; Type I            IPAs formed by Mo, W, V, Nb, Ta, or mixtures there of; Type            I HPAs formed by incorporation into the aforementioned IPAs            if any of the elements listed in Table II (heteroatoms)            either singly or in thereof; Or any HPA containing at least            one heteroatom type (i.e., element) contained in both Table            I and Table II;        -   d. the oxidizer species addressed in this patent are            combinations mediator species from any or all of these            generic groups;        -   e. the oxidizing species are super oxidizers and further            comprising creating secondary oxidizers by reacting the            super oxidizers with the aqueous anolyte;        -   f. an alkaline solution for aiding decomposing the            biological waste materials;        -   g. an alkaline solution for absorbing CO₂ and forming alkali            metal bicarbonate/carbonate for circulating through the            electrochemical cell for producing a percarbonate oxidizer;        -   h. using oxidizing species from the MEO process inorganic            free radicals generatedin aqueous solutions derived from            carbonate, azide, nitrite, nitrate, phosphite, phosphate,            sulfite, sulfate, selenite, thiocyanate, chloride, bromide,            iodide, and formate oxidizing species;        -   i. organic free radicals for aiding the MEO process and            breaking down the biological waste materials into simpler            (i.e., smaller molecular structure) organic compounds;        -   j. anions with an oxidation potential above a threshold            value of 1.7 volts (i.e., superoxidizer) for involving in a            secondary oxidation process for producing oxidizers;        -   k. The oxidizer species addressed in this patent (I.e.,            characteristic elements having atomic number below 90) are            described in Table I (simple anions redox couple mediators):            Type I IPAs formed by Mo, W, V, Nb, Ta, or mixtures there            of; Type I HPAs formed by incorporation into the            aforementioned IPAs if any of the elements listed in Table            II (heteroatoms) either singly or in thereof; Or any HPA            containing at least one heteroatom type (i.e., element)            contained in both Table I and Table II or combinations            mediator species from any or all of these generic groups;        -   j. the use of Ultrasonic energy induce microscopic bubble            implosion which will be used to affect a desired reduction            in sized of the individual second phase waste volumes            dispersed in the anolyte;        -   k. membrane can be microporous polymer, ceramic or glass            frit        -   l. with the possible impression of an AC voltage upon the DC            voltage to retard the formation of cell performance limiting            surface films on the electrode; and        -   m. external air is introduced through an air sparge into the            catholyte reservoir where oxygen contained in the air            oxidizes nitrous acid and the small amounts of nitrogen            oxides (NO_(x)), produced by the cathode reactions (this is            necessary only when HNO₃ ⁻ or NO₃ ⁻ salts can occur in the            catholyte)    -   12. The apparatus of paragraph 10, wherein:    -   a. each of the oxidizing species has normal valence states        (i.e., reduced form of redox couple) and higher valence        oxidizing states and further comprising creating the higher        valence oxidizing states (i.e., oxidized form of redox couple)of        the oxidizing species by stripping and reducing electrons off        normal valence state species in the electrochemical cell;        -   b. using species that are usable in alkaline solutions since            oxidation potentials of redox reactions producing hydrogen            ions are inversely related to pH which reduces the            electrical power required to destroy the biological waste;        -   c. further oxidizing species, and attacking specific organic            molecules with the oxidizing species while operating at            temperatures sufficiently low so as to preventing the            formation of dioxins and furans;        -   d. energizing the electrochemical cell at a potential level            sufficient to form the oxidized form of the redox couple            having the highest oxidation potential in the anolyte;        -   e. lower the temperature (e.g. between 0° C. and room            temperature) of the anolyte with the heat exchanger before            it enters the electrochemical cell to enhance the generation            of the oxidized form of the anion redox couple mediator; and        -   f. raise the temperature of the anolyte entering the anolyte            reaction chamber with the heat exchanger to affect the            desired chemical reactions at the desired rates following            the lowering of the temperature of the anolyte entering the            electrochemical cell.    -   13. The apparatus of paragraph 10, wherein:        -   a. the oxidizing species are one or more Type I            isopolyanions (i.e., complex anion redox couple mediators)            containing tungsten, molybdenum, vanadium, niobium,            tantalum, or combinations thereof as addenda atoms in            aqueous solution and the electrolyte is an acid, neutral or            alkaline aqueous solution;        -   b. the oxidizing species are one or more Type I            heteropolyanions formed by incorporation into the            aforementioned isopolyanions, as heteroatoms, any of the            elements listed in Table II, either singly or in combination            thereof in the aqueous solutions and the electrolyte is an            acid, neutral, or alkaline aqueous solution;        -   c. the oxidizing species are one or more of any            heteropolyanions containing at least one heteroatom type            (i.e., element) contained in both Table I and Table II in            the aqueous solutions_and the_electrolyte is an acid,            neutral, or alkaline aqueous solution;        -   d. the oxidizing species are combinations of anion redox            couple mediators from any or all of the previous four            subparagraphs (13a., 13b., 13c., 13d);        -   e. the oxidizing species are higher valence state of species            found in situ for destroying the biological waste material;            and        -   f. the electrolyte is an acid, neutral, or alkaline aqueous            solution.    -   14. The apparatus of paragraph 10, further comprising:        -   a. the aqueous solution is chosen from acids such as but not            limited to nitric acid, sulfuric acid, or phosphoric acid;            alkalines such as but not limited to of sodium hydroxide or            potassium hydroxide; or neutral electrolytes such as but not            limited to sodium or potassium nitrates, sulfates, or            phosphates;        -   b. sharps and the biological waste material is waste from            veterinary industry as identified under the definition of            biological waste hereto referred;        -   c. free hydroxyl radical for replacing hydrogen peroxide and            ozone in chemical sterilization;        -   d. a with a hydrogen or hydronium semipermeable, microporous            polymer, ceramic or glass frit membrane for separating the            anolyte portion and the catholyte portion while allowing            hydrogen or hydronium ion passage from the anolyte to the            catholyte;        -   e. oxidation potentials of redox reactions producing            hydrogen ions are inversely related to pH;        -   f. the biological waste is liquid waste;        -   g. the biological waste is a combination of liquids and            solids; and        -   h. oxidizing species may be interchanged in a preferred            embodiment without changing equipment.    -   15. The apparatus of paragraph 10, further comprising:        -   a. a anolyte reaction chamber(s) 5(b,c) and buffer tank 20            housing the bulk of the anolyte portion and the foraminous            basket 3;        -   b. a anolyte reaction chamber 5 a housing the bulk of the            anolyte portion;        -   c. a anolyte reaction chamber 5 d and buffer tank 20 housing            the bulk of the anolyte portion;        -   d. a spray head 4(a) and a stream head 4(b) attached to the            tubing coming from the electrochemical cell 25 that inputs            the anolyte containing the oxidizer into the anolyte            reaction chamber(s) 5(a,b,c) and buffer tank 20 in such a            manner as to promote mixing of the incoming anolyte with the            anolyte already in the anolyte reaction chambers(s) 5            (a,b,c);        -   e. a anolyte reaction chamber(s) 5(b,c) houses a foraminous            basket 3 with a top that holds sharps and solid biological            waste in the electrolyte;            a hinged lid 1 attached to the anolyte reaction chamber(s)            5(a,b,c) allowing insertion of waste into the anolyte            portion as liquid, solid, or a mixture of liquids and            solids;        -   f. the lid 1 contains an locking latch 76 to secure the            anolyte reaction chamber(s) 5(a,b,c) during operation;        -   g. a suction pump 8 is attached to buffer tank 20 to pump            anolyte to the anolyte reaction chamber(s) 5(c,d);        -   h. an input pump 10 to pump anolyte from the anolyte            reaction chamber(s) 5(c,d) back into the buffer tank 20; and        -   i. an air pump 32 to pump off gases from the anolyte            reaction chamber(s) 5(c,d) back into the buffer tank 20 for            further oxidation.    -   16. The apparatus of paragraph 10, further comprising:        -   a. an ultraviolet source 11 connected to the anolyte            reaction chamber(s) 5(a,b,c) and buffer tank 20 and            decomposing hydrogen peroxide and ozone into hydroxyl free            radicals therein and increasing efficiency of the MEO            process by recovering energy through the oxidation of sharps            and biological waste materials in the anolyte chamber by            these secondary oxidizers;        -   b. an ultrasonic source 9 connected to the anolyte reaction            chamber(s) 5(a,b,c) and buffer tank 20 for augmenting            secondary oxidation processes by heating the hydrogen            peroxide containing electrolyte to produce extremely short            lived and localized conditions of 4800° C. and 1000            atmospheres pressure within the anolyte to dissociate            hydrogen peroxide into hydroxyl free radicals thus            increasing the oxidation processes;        -   c. an ultrasonic energy 9 source connected into the anolyte            reaction chamber(s) 5(a,b,c) and buffer tank 20 for            irradiating cell membranes in biological waste materials by            momentarily raising temperature within the cell membranes            and causing cell membrane fail and rupture thus creating            greater exposure of cell contents to oxidizing species in            the anolyte;        -   d. the use of ultrasonic energy for mixing material in the            anolyte, via the ultrasonic energy source 9, to induce            microscopic bubble implosion which is used to affect a            desired reduction in sized of the individual second phase            waste volumes and disperse throughout the anolyte;        -   e. a mixer 35 for stirring the anolyte connected to the            anolyte reaction chamber(s) 5(a,b,c) and the buffer tank 20;        -   f. a CO₂ vent 14 for releasing CO₂ atmospherically;        -   g. the Sharps II container 34 is placed in the basket 3 in            anolyte reaction chamber(s) 5(b,c) to hold Sharps II and            used to remove them when the process is complete;        -   h. an inorganic compounds removal and treatment system 15            connected to the anolyte reaction chamber(s) 5(a,b,c) and            buffer tank 20 is used should there be more than trace            amount of chlorine, or other precipitate forming anions            present in the sharps and biological waste being processed,            thereby precluding formation of unstable oxycompounds (e.g.,            perchlorates, etc.);        -   i. an gas cleaning system 16 comprises scrubber/absorption            columns;        -   j. the condenser 13 connected to the anolyte reaction            chamber(s) 5(a,b,c) and buffer tank 20;        -   k. non-condensable incomplete oxidation products (e.g., low            molecular weight organics, carbon monoxide, etc.) are            reduced to acceptable levels for atmospheric release by a            gas cleaning system 16;        -   l. gas cleaning system 16 is not a necessary component of            the MEO apparatus for the destruction of most types of            biological waste;        -   m. when the gas cleaning system 16 is incorporated into the            MEO apparatus, the anolyte off-gas is contacted in a gas            cleaning system 16 wherein the noncondensibles from the            condenser 13 are introduced into the lower portion of the            gas cleaning system 16 through a flow distribution system            and a small side stream of freshly oxidized anolyte direct            from the electrochemical cell 25 is introduced into the            upper portion of the column, this results in the gas phase            continuously reacting with the oxidizing mediator species as            it rises up the column past the downflowing anolyte;        -   n. external drain 12, for draining to the organic compound            removal system 17 and the inorganic compounds removal and            treatment system 15, and for draining the anolyte system;        -   o. organic compounds recovery system 17 is used to            recover a) organic materials that are benign and do not need            further treatment, and b) organic materials that is used in            the form they have been reduced and thus would be recovered            for that purpose;        -   p. small thermal control units 21 and 22 are connected to            the flow stream to heat or cool the anolyte to the selected            temperature range;        -   q. anolyte is circulated into the anolyte reaction            chamber(s) 5(a,b,c,d) and buffer tank 20 through the            electrochemical cell 25 by pump 19 on the anode 26 side of            the membrane 27;        -   r. a flush(s) 18 for flushing the anolyte and catholyte            systems;        -   s. filter 6 is located at the base of the anolyte reaction            chambers 5(a,b,c,d) and buffer tank 20 to limit the size of            the solid particles to approximately 1 mm in diameter;        -   t. membrane 27 in the electrochemical cell 25 separates the            anolyte portion and catholyte portion of the electrolyte;        -   u. electrochemical cell 25 is energized by a DC power supply            29, which is powered by the AC power supply 30;        -   v. DC power supply 29 is low voltage high current supply            usually operating below 4v DC but not limited to that range;        -   w. AC power supply 29 operates off a typical 110v AC line            for the smaller units and 240v AC for the larger units;        -   x. electrolyte containment boundary is composed of materials            resistant to the oxidizing electrolyte (e.g., PTFE, PTFE            lined tubing, glass, etc.); and        -   y. an electrochemical cell 25 connected to the anolyte            reaction chamber(s) 5(a,b,c) and buffer tank 20.    -   17. The apparatus of paragraph 10, wherein:        -   a. in the anolyte reaction chambers 5(a,b,c) and buffer tank            20 is the aqueous acid, alkali, or neutral salt electrolyte            and mediated oxidizer species solution in which the oxidizer            form of the mediator redox couple initially may be present            or may be generated electrochemically after introduction of            the sharps and biological waste and application of DC power            29 to the electrochemical cell 25;        -   b. sharps and biological waste is introduced when the            anolyte is at room temperature, operating temperature or            some optimum intermediate temperature;        -   c. DC power supply 29 provides direct current to an            electrochemical cell 25;        -   d. pump 19 circulates the anolyte portion of the electrolyte            and the sharps and biological waste is rapidly oxidized at            temperatures below 100° C. and ambient pressure;        -   e. in-line filter 6 prevents solid particles large enough to            clog the electrochemical cell 25 flow paths from exiting            this reaction chamber(s) 5(a,b,c,d) and buffer tank 20;        -   f. residue is pacified in the form of a salt and may be            periodically removed through the Inorganic Compound Removal            and Treatment System 15 and drain outlets 12;        -   g. electrolyte may be changed through this same plumbing for            introduction into the reaction chamber(s) 5(a,b,c) and            buffer tank 20 and 31;        -   h. the process operates at low temperature and ambient            atmospheric pressure and does not generate toxic compounds            during the destruction of the biological waste, making the            process indoors compatible;        -   i. the system is scalable to a unit suitable for a large            industrial application; and        -   j. CO₂ oxidation product from the anolyte system A is vented            out the CO₂ vent 14.    -   18. The apparatus of paragraph 10, wherein:        -   a. an anolyte recovery system 41 connected to the catholyte            pump (43);        -   b. a thermal control unit 45 connected to the catholyte            reservoir for varying the temperature of the catholyte            portion;        -   c. a catholyte reservoir 31 connected to the cathode portion            of the electrochemical cell;        -   d. bulk of the catholyte is resident in the catholyte            reaction chamber 31;        -   e. catholyte portion of the electrolyte flows into a            catholyte reservoir 31;        -   f. an air sparge 37 connected to the catholyte reservoir 31            for introducing air into the catholyte reservoir 31;        -   g. an anolyte recovery system 41 for capturing the anions            and for reintroducing the anions into the anolyte chamber(s)            5(a,b,c) and buffer tank 20 or disposal from the catholyte            electrolyte;        -   h. an off gas cleaning system 39 for cleaning gases before            release into the atmosphere connected to the catholyte            reservoir 31;        -   i. an atmospheric vent 47 for releasing gases into the            atmosphere connected to the off gas cleaning system 39;        -   j. cleaned gas from the off gas cleaning system 39 is            combined with unreacted components of the air introduced            into the system and discharged through the atmospheric vent            47;        -   k. a catholyte reservoir 31 has a screwed top 33 (shown in            FIG. 1A), which allow access to the reservoir 31 for            cleaning and maintenance by service personnel;        -   l. a mixer 35 for stirring the catholyte connected to the            catholyte reservoir 31;        -   m. a catholyte pump 43 for circulating catholyte back to the            electrochemical cell 25 connected to the catholyte reservoir            31;        -   n. a drain 12 for draining catholyte;        -   o. a flush 18 for flushing the catholyte system;        -   p. an air sparge 37 connected to the housing for introducing            air into the catholyte reaction chamber 31;        -   q. catholyte portion of the electrolyte is circulated by            pump 43 through the electrochemical cell 25 on the cathode            28 side of the membrane 27;        -   r. small thermal control units 45 and 46 are connected to            the catholyte flow stream to heat or cool the catholyte to            the selected temperature range;        -   s. contact of the oxidizing gas with the catholyte            electrolyte may be enhanced by using conventional techniques            for promoting gas/liquid contact by a ultrasonic vibration            48, a mechanical mixer 35, etc.;        -   t. operating the electrochemical cell 25 at higher than            normal membrane 27 current densities (i.e., above about 0.5            amps/cm²) will increase the rate of waste destruction, but            also result in increased mediator ion transport through the            membrane into the catholyte;        -   u. optional anolyte recovery system 41 is positioned on the            catholyte side;        -   v. systems using non-nitric acid catholytes may also require            air sparging to dilute and/or remove off-gas such as            hydrogen;        -   w. some mediator oxidizer ions may cross the membrane 27 and            this option is available if it is necessary to remove them            through the anolyte recovery system 41 to maintain process            efficiency or cell operability, or their economic worth            necessitates their recovery;        -   x. using the anolyte recovery system 41 the capitol cost of            expanding the size of the electrochemical cell 25 can be            avoided; and        -   y. operating the electrochemical cell 25 at higher than            normal membrane current density (i.e., above about 0.5 amps            per centimeter squared) improves economic efficiency.    -   19. The apparatus of paragraph 10, wherein:        -   a. operator runs the MEO Apparatus (FIG. 1A) and FIG. 1B by            using the MEO Controller depicted in FIG. 3 MEO Controller;        -   b. controller 49 with microprocessor is connected to a            monitor 51 and a keyboard 53;        -   c. operator inputs commands to the controller 49 through the            keyboard 53 responding to the information displayed on the            monitor 51;        -   d. controller 49 runs a program that sequences the steps for            the operation of the MEO apparatus;        -   e. program has pre-programmed sequences of standard            operations that the operator may follow or may choose his            own sequences of operations;        -   f. controller 49 allows the operator to select his own            sequences within limits that assure a safe and reliable            operation;        -   g. controller 49 sends digital commands that regulates the            electrical power (AC 30 and DC 29) to the various components            in the MEO apparatus: pumps 19 and 43, mixers 7 and 35,            thermal controls 21, 22, 45, 46, heat exchangers 23 and 24,            ultraviolet sources 11, ultrasonic sources 9 and 48, CO₂            vent 14, air sparge 37, and electrochemical cell 25;        -   h. controller receives component response and status from            the components;        -   i. controller sends digital commands to the sensors to            access sensor information through sensor responses;        -   j. sensors in the MEO apparatus provide digital information            on the state of the various components;        -   k. sensors measure flow rate 59, temperature 61, pH 63, CO₂            venting 65, degree of oxidation 67, air sparge sensor 69,            etc; and        -   l. controller 49 receives status information on the            electrical potential (voltmeter 57) across the            electrochemical cell or individual cells if a multi-cell            configuration and between the anode(s) and reference            electrodes internal to the cell(s) 25 and the current            (ammeter 55) flowing between the electrodes within each            cell.    -   20. The apparatus of paragraph 10, wherein:        -   a. preferred embodiment, MEO System Model 5.b is sized for            use in a small to mid-size application; other preferred            embodiments have differences in the external configuration            and size but are essentially the same in internal function            and components as depicted in FIGS. 1B, 1C, 1D, and 1E;        -   b. preferred embodiment in FIG. 3 comprises a housing 72            constructed of metal or high strength plastic surrounding            the electrochemical cell 25, the electrolyte and the            foraminous basket 3;        -   c. AC power is provided to the AC power supply 30 by the            power cord 78;        -   d. monitor screen 51 is incorporated into the housing 72 for            displaying information about the system and about the waste            being treated;        -   e. control keyboard 53 is incorporated into the housing 72            for inputting information into the system;        -   f. monitor screen 51 and the control keyboard 53 may be            attached to the system without incorporating them into the            housing 72;        -   g. system model 5.b has a control keyboard 53 for input of            commands and data;        -   h. monitor screen 51 to display the systems operation and            functions;        -   i. status lights 73 for on, off and standby, are located            above the keyboard 53 and monitor screen 51;        -   j. in a preferred embodiment, status lights 73 are            incorporated into the housing 72 for displaying information            about the status of the treatment of the sharps and            biological waste material;        -   k. air sparge 37 is incorporated into the housing 72 to            allow air to be introduced into the catholyte reaction            chamber 31 below the surface of the catholyte;        -   l. a CO₂ vent 14 is incorporated into the housing 72 to            allow for CO₂ release from the anolyte reaction chamber            housed within;        -   m. in a preferred embodiment, the housing includes means for            cleaning out the MEO waste treatment system, including a            flush(s) 18 and drain(s) 12 through which the anolyte and            catholyte pass;        -   n. the preferred embodiment further comprises an atmospheric            vent 47 facilitating the releases of gases into the            atmosphere from the catholyte reaction chamber 31;        -   o. hinged lid 1 is opened and the sharps and biological            waste is deposited in the basket 3 in the chamber 5 b;        -   p. lid stop 2 keeps lid opening controlled; and        -   q. hinged lid 1 is equipped with a locking latch 76 that is            operated by the controller 49.    -   21. The apparatus of paragraph 10, wherein:        -   a. MEO apparatus is contained in the housing 72;        -   b. MEO system is started 81 by the operator engaging the            ‘ON’ button 74 on the control keyboard 53;        -   c. system controller 49, which contains a microprocessor,            runs the program that controls the entire sequence of            operations 82;        -   d. monitor screen 51 displays the steps of the process in            the proper sequence;        -   e. status lights 73 on the panel provide the status of the            MEO apparatus (e.g. on, off, ready, standby);        -   f. lid 1 is opened and the sharps and infectious waste is            placed 83 in the anolyte reaction chamber 5 b in basket 3 as            a liquid, solid, or a mixture of liquids and solids,            whereupon the solid portion of the waste is retained and the            liquid portion flows through the basket and into the            anolyte;        -   g. locking latch 76 is activated after waste is placed in            basket;        -   h. pumps 19 and 43 are activated which begins circulation 85            of the anolyte 87 and catholyte 89, respectively;        -   i. once the electrolyte circulation is established            throughout the system, the mixers 7 and 35 begin to operate            91 and 93;        -   j. depending upon waste characteristics (e.g., reaction            kinetics, heat of reaction, etc.) it may be desirable to            introduce the waste into the anolyte at room temperature or            cooler in the MEO system with little or none of the mediator            redox couple in the oxidizer form;        -   k. once flow is established the thermal controls units 21,            22, 45, and 46 are turned on 95/97, initiating predetermined            anodic oxidation and electrolyte heating programs;        -   l. the electrochemical cell 25 is energized 94 (by cell            commands 56) to the electric potential 57 and current 55            density determined by the controller program;        -   m. by using programmed electrical power and electrolyte            temperature ramps it is possible to maintain a predetermined            waste destruction rate profile such as a relatively constant            reaction rate as the more reactive waste components are            oxidized, thus resulting in the remaining waste becoming            less and less reactive, thereby requiring more and more            vigorous oxidizing conditions;        -   n. the ultrasonic sources 9 and 48 and ultraviolet systems            11 are activated 99 and 101 in the anolyte reaction chambers            5(a,b,c) and buffer tank 20 and catholyte reaction chamber            31 if those options are chosen in the controller program;        -   o. CO₂ vent 14 is activated 103 to release CO₂ from the            biological waste oxidation process in the anolyte reaction            chamber(s) 5(a,b,c) and buffer tank 20;        -   p. air sparge 37 and atmospheric vent 47 are activated 105            in the catholyte system;        -   q. progress of the destruction process is monitored in the            controller,(oxidation sensor 67) by various cell voltages            and currents 55, 57 (e.g., open circuit, anode vs. reference            electrode, ion specific electrodes, etc,) as well as            monitoring CO₂, CO, and O₂ gas 65 composition for CO₂, CO            and oxygen content;        -   r. infectious waste is being decomposed into water and CO₂            the latter being discharged 103 out of the CO₂ vent 14;        -   s. air sparge 37 draws air 105 into the catholyte reservoir            31, and excess air is discharged out the atmospheric vent            47;        -   t. when the oxidation sensor 67 determine the desired degree            of infectious waste destruction has been obtained 107, the            system goes to standby 109;        -   u. MEO apparatus as an option may be placed in a standby            mode with infectious waste being added as it is generated            throughout the day and the unit placed in full activation            during non-business hours; and

v. system operator executes system shutdown 111 using the controllerkeyboard 53. TABLE I SIMPLE ANION REDOX COUPLES MEDIATORS SUB GROUPGROUP ELEMENT VALENCE SPECIES SPECIFIC REDOX COUPLES I A None B Copper(Cu) +2 Cu⁻² (cupric) +2 Species/+3, +4 Species HCuO₂ (bicuprite) +3Species/+4 Species CuO₂ ⁻² (cuprite) +3 Cu⁺³ CuO₂ ⁻ (cuprate) Cu₂O₃(sesquioxide) +4 CuO₂ (peroxide) Silver (Ag) +1 Ag⁺ (argentous) +1Species/+2, +3 Species AgO⁻ (argentite) +2 Species/+3 Species +2 Ag⁻²(argentic) AgO (argentic oxide) +3 AgO⁺ (argentyl) Ag₂O₃ (sesquioxide)Gold (Au) +1 Au⁺ (aurous) +1 Species/+3, +4 Species +3 Au⁺³ (auric) +3Species/+4 Species AuO⁻ (auryl) H₃AuO₃ ⁻ (auric acid) H₂AuO₃ ⁻(monoauarate) HAuO₃ ⁻² (diaurate) AuO₃ ⁻³ (triaurate) Au₂O₃ (auricoxide) Au(OH)₃ (auric hydroxide) +4 AuO₂ (peroxide) II A Magnesium (Mg)+2 Mg⁺² (magnesic) +2 Species/+4 Species +4 MgO₂ (peroxide) Calcium (Ca)+2 Ca⁺² +2 Species/+4 Species +4 CaO₂ (peroxide) Strontium +2 Sr⁺² +2Species/+4 Species +4 SrO₂ (peroxide) Barium (Ba) +2 Ba⁺² +2 Species/+4Species +4 BaO₂ (peroxide) II B Zinc (Zn) +2 Zn⁺² (zincic) +2 Species/+4Species ZnOH¹ (zincyl) HZnO₂ ⁻(bizincate) ZnO₂ ⁻² (zincate) +4 ZnO₂(peroxide) Mercury (Hg) +2 Hg⁺² (mercuric) +2 Species/+4 Species Hg(OH)₂(mercuric hydroxide) HHgO₂ ⁻ (mercurate) +4 HgO₂ (peroxide) III A Boron+3 H₃BO₃ (orthoboric acid) +3 Species/+4.5, +5 Species H₂BO₃ ⁻, HBO₃ ⁻²,BO₃ ⁻³ (orthoborates) BO₂ ⁻ (metaborate) H₂B₄O₇ (tetraboric acid) HB₄O₇⁻/B₄O₇ ⁻² (tetraborates) B₂O₄ ⁻² (diborate) B₆O₁₀ ⁻² (hexaborate) +4.5B₂O₅ ⁻ (diborate) +5 BO₃ ⁻/BO₂ ⁻·H₂O (perborate) Thallium (Tl) +1 Tl⁺¹(thallous) +1 Species/+3 or +3.33 Species +3 Tl⁺³ (thallic) +3Species/+3.33 Species TlO⁺, TlOH⁺², Tl(OH)₂ ⁺ (thallyl) Tl₂O₃(sesquioxide) Tl(OH)₃ (hydroxide) +3.33 Tl₃O₅ (peroxide) B See RareEarths and Actinides IV A Carbon (C) +4 H₂CO₃(carbonic acid) +4Species/+5, +6 Species HCO₃ ⁻ (bicarbonate) CO₃ ⁻² (carbonate) +5 H₂C₂O₆(perdicarbonic acid) +6 H₂CO₄(permonocarbonic acid) Germanium (Ge) +4H₂GeO₃ (germanic acid) +4 Species/+6 Species HGeO₃ ⁻ (bigermaniate) GeO₃⁻⁴ (germinate) Ge⁺⁴ (germanic) GeO₄ ⁻⁴ H₂Ge₂O₅ (digermanic acid) H₂Ge₄O₉(tetragermanic acid) H₂Ge₅O₁₁ (pentagermanic acid) HGe₅O₁₁ ⁻(bipentagermanate) +6 Ge₅O₁₁ ⁻² (pentagermanate) Tin (Sn) +4 Sn⁺⁴(stannic) +4 Species/+7 Species HSnO₃ ⁻ (bistannate) SnO₃ ⁻² (stannate)SnO₂ (stannic oxide) Sn(OH)₄ (stannic hydroxide) +7 SnO₄ ⁻ (perstannate)Lead (Pb) +2 Pb⁺² (plumbous) +2, +2.67, +3 Species/+4 Species HPbO₂ ⁻(biplumbite) PbOH⁺ PbO₂ ⁻² (plumbite) PbO (plumbus oxide) +2.67 Pb₃O₄(plumbo-plumbic oxide) +3 Pb₂O₃ (sequioxide) IV A Lead (Pb) +4 Pb⁺⁴(plumbic) +2, +2.67, +3 Species/+4 Species PbO₃ ⁻² (metaplumbate) HPbO₃⁻ (acid metaplumbate) PbO₄ ⁻⁴ (orthoplumbate) PbO₂ (dioxide) B Titanium+4 TiO⁺² (pertitanyl) +4 Species/+6 Species HTiO₄ ⁻ titanate) TiO₂(dioxide) +6 TiO₂ ⁺² (pertitanyl) HTiO₄ ⁻ (acid pertitanate) TiO₄ ⁻²(pertitanate) TiO₃ (peroxide) Zirconium (Zr) +4 Zr⁺⁴ (zirconic) +4Species/+5, +6, +7 Species ZrO⁺² (zirconyl) HZrO₃ ⁻ (zirconate) +5 Zr₂O₅(pentoxide) +6 ZrO₃ (peroxide) +7 Zr₂O₇ (heptoxide) Hafnium (Hf) +4 Hf⁺⁴(hafnic) +4 Species/+6 Species HfO⁺² (hafnyl) +6 HfO₃ (peroxide) V ANitrogen +5 HNO₃ (nitric acid) +5 species/+7 Species NO₃ ⁻ (nitrate) +7HNO₄ (pernitric acid) Phosphorus (P) +5 H₃PO₄ (orthophosphoric acid) +5Species/+6, +7 species H₂PO₄ ⁻ (monoorthophosphate) HPO₄ ⁻²(diorthophosphate) PO₄ ⁻³ (triorthophosphate) HPO₃ (metaphosphoric acid)H₄P₂O₇ (pryophosphoric acid) H₅P₃O₁₀ (triphosphoric acid) H₆P₄O₁₃(tetraphosphoric acid) V A Phosphorus (P) +6 H₄P₂O₈ (perphosphoric acid)+5 Species/+6, +7 Species +7 H₃PO₅ (monoperphosphoric acid) Arsenic (As)+5 H₃AsO₄ (ortho-arsenic acid) +5 Species/+7 species H₂AsO₄ ⁻ (monoortho-arsenate) HAsO₄ ⁻² (di-ortho-arsenate) AsO₄ ⁻³(tri-ortho-arsenate) AsO₂ ⁺ (arsenyl) +7 AsO₃ ⁺ (perarsenyl) Bismuth(Bi) +3 Bi⁺³ (bismuthous) +3 Species/+3.5, +4, +5 Species BiOH⁺²(hydroxybismuthous) BiO⁺ (bismuthyl) BiO₂ ⁺(metabismuthite) +3.5 Bi₄O₇(oxide) +4 Bi₂O₄ (tetroxide) +5 BiO₃ ⁻ (metabismuthite) Bi₂O₅(pentoxide) B Vanadium (V) +5 VO₂ ⁺ (vanadic) +5 Species/+7, +9 Species(See also POM H₃V₂O₇ ⁻ (pyrovanadate) Complex Anion H₂VO₄ ⁻(orthovanadate) Mediators) VO₃ ⁻ (metavanadate) HVO₄ ⁻² (orthovanadate)VO₄ ⁻³ (orthovanadate) V₂O₅ (pentoxide) H₄V₂O₇ (pyrovanadic acid) HVO₃(metavanadic acid) H₄V₆O₁₇ (hexavanadic acid) +7 VO₄ ⁻ (pervanadate) +9VO₅ ⁻ (hypervanadate) VI B Chromium +3 Cr⁺³ (chromic) +3 Species/+4, +6Species CrOH⁺², Cr(OH)₂ ⁺ (chromyls) +4 Species/+6 Species CrO₂ ⁻, CrO₃⁻³ (chromites) Cr₂O₃ (chromic oxide) Cr(OH)₃ (chromic hydroxide) +4 CrO₂(dioxide) Cr(OH)₄ (hydroxide) +6 H₂CrO₄ (chromic acid) HCrO₄ ⁻ (acidchromate) CrO₄ ⁻² (chromate) Cr₂O₇ ⁻² (dichromate) Molybdenum (Mo) +6HMoO₄ ⁻ (bimolybhate) +6 Species/+7 Species (See also POM MoO₄ ⁻²(molydbate) Complex Anion MoO₃ (molybdic trioxide) Mediators) H₂MoO₄(molybolic acid) +7 MoO₄ ⁻ (permolybdate) Tungsten (W) +6 WO₄ ⁻²tungstic) +6 Species/+8 Species (See also POM WO₃ (trioxide) ComplexAnion H₂WO₄ (tungstic acid) Mediators) +8 WO₅ ⁻² (pertungstic) H₂WO₅(pertungstic acid) VII A Chlorine (Cl) −1 Cl⁻ (chloride) −1 Species/+1,+3, +5, +7 Species +1 HClO (hypochlorous acid) +1 Species/+3, +5, +7Species ClO⁻ (hypochlorite) +3 Species/+5, +7 Species +3 HClO₂ (chlorousacid) +5 Species/+7 Species ClO₂ ⁻ (chlorite) +5 HClO₃ (chloric acid)ClO₃ ⁻ (chlorate) +7 HClO₄ (perchloric acid) ClO₄ ⁻, HClO₅ ⁻², ClO₅ ⁻³,Cl₂O₉ ⁻⁴ (perchlorates) V B Niobium (Nb) +5 NbO₃ ⁻ (metaniobate) +5Species/+7 species (See also POM NbO₄ ⁻³ (orthoniobate) Complex AnionNb₂O₅ (pentoxide) Mediators) HNbO₃ (niobid acid) +7 NbO₄ ⁻ (perniobate)Nb₂O₇ (perniobic oxide) HNbO₄ (perniobic acid) Tantalum (Ta) +5 TaO₃ ⁻(metatantalate) +5 species/+7 species (See also POM TaO₄ ⁻³(orthotanatalate) Complex Anion Ta₂O₅ (pentoxide) Mediators) HTaO₃(tantalic acid) +7 TaO₄ ⁻ (pentantalate) Ta₂O₇ (pertantalate) HTaO₄·H₂O(pertantalic acid) VI A Sulfur (S) +6 H₂SO₄ (sulfuric acid) +6Species/+7, +8 Species HSO₄ ⁻ (bisulfate) SO₄ ⁻² (sulfate) +7 S₂O₈ ⁻²(dipersulfate) +8 H₂SO₅ (momopersulfuric acid) Selenium (Se) +6 H₂Se₂O₄(selenic acid) +6 species/+7 Species HSeO₄ ⁻ (biselenate) SeO₄ ⁻²(selenate) +7 H₂Se₂O₈ (perdiselenic acid) Tellurium (Te) +6 H₂TeO₄(telluric acid) +6 species/+7 species HTeO₄ ⁻ (bitellurate) TeO₄ ⁻²(tellurate) +7 H₂Te₂O₈ (perditellenic acid) Polonium (Po) +2 Po⁺²(polonous) +2, +4 species/+6 Species +4 PoO₃ ⁻² (polonate) +6 PoO₃(peroxide) VII A Bromine (Br) −1 Br⁻ (bromide) −1 Species/+1, +3, +5, +7Species +1 HBrO (hypobromous acid) +1 Species/+3, +5, +7 Species BrO⁻(hypobromitee) +3 Species/+5, +7 Species +3 HBrO₂ (bromous acid) +5Species/+7 Species BrO2⁻ (bromite) +5 HBrO₃ (bromic acid) BrO₃ ⁻(bromate) +7 HBrO₄ (perbromic acid) BrO₄ ⁻, HBrO₅ ⁻², BrO₅ ⁻³, Br₂O₉ ⁻⁴(prebromates) Iodine −1 I⁻ (iodide) −1 Species/+1, +3, +5, +7 Species +1HIO (hypoiodus acid) +1 Species/+3, +5, +7 Species IO⁻ (hypoiodite) +3Species/+5, +7 Species +3 HIO₂ (iodous acid) +5 Species/+7 Species IO₂ ⁻(iodite) +5 HIO₃ (iodic acid) IO₃ ⁻ (iodate) +7 HIO₄ (periodic acid) IO₄⁻, HIO₅ ⁻², IO₅ ⁻³, I₂O₉ ⁻⁴ (periodates) B Manganese (Mn) +2 Mn⁺²(manganeous) +2 Species/+3, +4, +6, +7 Species HMnO₂ ⁻ (dimanganite) +3Species/+4, +6, +7 Species +3 Mn⁺³ (manganic) +4 Species/+6, +7 Species+4 MnO₂ (dioxide) +6 Species/+7 Species +6 MnO₄ ⁻² (manganate) +7 MnO₄ ⁻(permanganate) VIII Period 4 Iron (Fe) +2 Fe⁺² (ferrous) +2 Species/+3,+4, +5, +6 Species HFeO₂ ⁻ (dihypoferrite) +3 Species/+4, +5, +6 Species+3 Fe⁺³, FeOH⁺², +4 Species/+5, +6 Species Fe(OH)₂ ⁺ (ferric) +5Species/+6 Species FeO₂ ⁻ (ferrite) +4 FeO⁺² (ferryl) FeO₂ ⁻²(perferrite) +5 FeO₂ ⁺ (perferryl) +6 FeO₄ ⁻² (ferrate) Cobalt (Co) +2Co⁺² (cobalous) +2 Species/+3, +4 Species HCoO₂ ⁻ (dicobaltite) +3Species/+4 Species +3 Co⁺³ (cobaltic) Co₂O₃ (cobaltic oxide) +4 CoO₂(peroxide) H₂CoO₃ (cobaltic acid) Nickel (Ni) +2 Ni⁺² (nickelous) +2Species/+3, +4, +6 Species NiOH⁺ +3 Species/+4, +6 Species HNiO₂ ⁻(dinickelite) +4 Species/+6 Species NiO₂ ⁻² (nickelite) +3 Ni⁺³(nickelic) Ni₂O₃ (nickelic oxide) +4 NiO₂ (peroxide) +6 NiO₄ ⁻²(nickelate) VIII Period 5 Ruthenium (Ru) +2 Ru⁺² +2 Species/+3, +4, +5,+6, +7, +8 Species +3 Ru⁺³ +3 Species/+4, +5, +6, +7, +8 Species Ru₂O₃(sesquioxide) +4 Species/+5, +6, +7, +8 Species Ru(OH)₃ (hydroxide) +5Species/+6, +7, +8 Species +4 Ru⁺⁴ (ruthenic) +6 Species/+7, +8 SpeciesRuO₂ (ruthenic dioxide) +7 Species/+8 Species Ru(OH)₄ (ruthenichydroxide) +5 Ru₂O₅ (pentoxide) +6 RuO₄ ⁻² (ruthenate) RuO₂ ⁺²(ruthenyl) RuO₃ (trioxide) +7 RuO₄ ⁻ (perruthenate) +8 H₂RuO₄(hyperuthenic acid) HRuO₅ ⁻ (diperruthenate) RuO₄ (ruthenium tetroxide)Rhodium (Rh) +1 Rh⁺ (hyporhodous) +1 Species/+2, +3, +4, +6 Species +2Rh⁺² (rhodous) +2 Species/+3, +4, +6 Species +3 Rh⁺³ (rhodic) +3Species/+4, +6 Species Rh₂O₃ (sesquioxide) +4 Species/+6 Species +4 RhO₂(rhodic oxide) Rh(OH)₄ (hydroxide) +6 RhO₄ ⁻² (rhodate) RhO₃ (trioxide)Palladium +2 Pd⁺² (palladous) +2 Species/+3, +4, +6 Species PdO₂ ⁻²(palladite) +3 Species/+4, +6 Species +3 Pd₂O₃ (sesquioxide) +4Species/+6 Species +4 PdO₃ ⁻² (palladate) PdO₂ (dioxide) Pd(OH)₄(hydroxide) +6 PdO₃ (peroxide) VIII Period 6 Iridium (Ir) +3 Ir⁺³(iridic) +3 Species/+4, +6 Species Ir₂O₃ (iridium sesquioxide) +4Species/+6 Species Ir(OH)₃ (iridium hydroxide) +4 IrO₂ (iridic oxide)Ir(OH)₄ (iridic hydroxide) +6 IrO₄ ⁻² (iridate) IrO₃ (iridium peroxide)Platinum (Pt) +2 Pt⁺² (platinous) +2, +3 Species/+4, +6 Species +3 Pt₂O₃(sesquioxide) +4 Species/+6 Species +4 PtO₃ ⁻² (palatinate) PtO⁺²(platinyl) Pt(OH)⁺³ PtO₂ (platonic oxide) IIIB Rare earths Cerium (Ce)+3 Ce⁺³ (cerous) +3 Species/+4, +6 Species Ce₂O₃ (cerous oxide) +4Species/+6 Species Ce(OH)₃ (cerous hydroxide) +4 Ce⁺⁴, Ce(OH)⁺³, Ce(OH)₂⁺², Ce(OH)₃ ⁺ (ceric) CeO₂ (ceric oxide) +6 CeO₃ (peroxide) Praseodymium(Pr) +3 Pr⁺³ (praseodymous) +3 species/+4 species Pr₂O₃ (sesquioxide)Pr(OH)₃ (hydroxide) +4 Pr⁺⁴ (praseodymic) PrO₂ (dioxide) Neodymium +3Nd⁺³ +3 Species/+4 Species Nd₂O₃ (sesquioxide) +4 NdO₂ (peroxide)Terbium (Tb) +3 Tb⁺³ +3 Species/+4 Species Tb₂O₃ (sesquioxide) +4 TbO₂(peroxide) IIIB Actinides Thorium (Th) +4 Th⁺⁴ (thoric) +4 Species/+6Species ThO⁺² (thoryl) HThO₃ ⁻ (thorate) +6 ThO₃ (acid peroxide) Uranium(U) +6 UO₂ ⁺² (uranyl) +6 Species/+8 Species UO₃ (uranic oxide) +8 HUO₅⁻, UO₅ ⁻² (peruranates) UO₄ (peroxide) Neptunium (Np) +5 NpO₂ ⁺(hyponeptunyl) +5 Species/+6, +8 Species Np₂O₅ (pentoxide) +6 Species/+8Species +6 NpO₂ ⁺² (neptunyl) NpO₃ (trioxide) +8 NpO₄ (peroxide)Plutonium (Pu) +3 Pu⁺³ (hypoplutonous) +3 Species/+4, +5, +6 Species +4Pu⁺⁴ (plutonous) +4 Species/+5, +6 Species PuO₂ (dioxide) +5 Species/+6Species +5 PuO₂ ⁺ (hypoplutonyl) Pu₂O₅ (pentoxide) +6 PuO₂ ⁺² (plutonyl)PuO₃ (peroxide) Americium (Am) +3 Am⁺³ (hypoamericious) +4 Am⁺⁴(americous) AmO₂ (dioxide) Am(OH)₄ (hydroxide) +5 AmO₂ ⁺ (hypoamericyl)Am₂O₅ (pentoxide) +6 AmO₂ ⁺² (americyl) AmO₃ (peroxide)

TABLE II ELEMENTS PARTICIPATING AS HETEROATOMS IN HETEROPOLYANIONCOMPLEX ANION REDOX COUPLE MEDIATORS SUB GROUP GROUP ELEMENT I A Lithium(Li), Sodium (Na), Potassium (K), and Cesium (Cs) B Copper (Cu), Silver(Ag), and Gold (Au) II A Beryllium (Be), Magnesium (Mg), Calcium (Ca),Strontium (Sr), and Barium (Ba) B Zinc (Zn), Cadmium (Cd), and Mercury(Hg) III A Boron (B), and Aluminum (Al) B Scandium (Sc), and Yttrium(Y) - (See Rare Earths) IV A Carbon (C), Silicon (Si), Germanium (Ge),Tin (Sn) and Lead (Pb) B Titanium (Ti), Zirconium (Zr), and Hafnium (Hf)V A Nitrogen (N), Phosphorous (P), Arsenic (As), Antimony (Sb), andBismuth (Bi) B Vanadium (V), Niobium (Nb), and Tantalum (Ta) VI A Sulfur(S), Selenium (Se), and Tellurium (Te) B Chromium (Cr), Molybdenum (Mo),and Tungsten (W) VII A Fluorine (F), Chlorine (Cl), Bromine (Br), andIodine (I) B Manganese (Mn), Technetium (Tc), and Rhenium (Re) VIIIPeriod 4 Iron (Fe), Cobalt (Co), and Nickel (Ni) Period 5 Ruthenium(Ru), Rhodium (Rh), and Palladium (Pd) Period 6 Osmium (Os), Iridium(Ir), and Platinum (Pt) IIIB Rare All Earths

1. A process for treating and oxidizing Sharps I and sterilizing SharpsII and biological waste materials comprising disposing an electrolyte inan electrochemical cell, separating the electrolyte into an anolyteportion and a catholyte portion with an ion-selective membrane orsemipermeable membrane applying a direct current voltage between theanolyte portion and the catholyte portion, placing the sharps andbiological waste in the anolyte portion, oxidizing the Sharps I intometallic ions in solution in the anolyte, sterilizing Sharps II, andbiological waste in the anolyte portion with a mediated electrochemicaloxidation (MEO) process, wherein the anolyte portion further comprises amediator in aqueous solution and the electrolyte is an acid, neutral oralkaline aqueous solution.
 2. The process of claim 1, wherein themediator is selected from the group of mediators described in Table I.3. The process of claim 1, wherein the oxidizing species are selectedfrom one or more of a group of Type I complex anion redox coupleisopolyanion mediators containing tungsten, molybdenum, vanadium,niobium, tantalum, or combinations thereof as addenda atoms in aqueoussolution.
 4. The process of claim 1, wherein the oxidizing species areselected from one or more of a group of Type I heteropolyanions formedby incorporation into Type I isopolyanions, as heteroatoms, any of theelements listed in Table II, either singly or in combination thereof inthe aqueous solution.
 5. The process of claim 1, wherein the oxidizingspecies are selected from one or more of a group of heteropolyanionscontaining at least one heteroatom type element contained in both TableI and Table II in the aqueous solution.
 6. The process of claim 1,wherein the oxidizing species are selected from a group of combinationsof anion redox couple mediators described in Tables I and II, andwherein reduced forms of the redox couples are reoxidized in the anolyteportion within the electrochemical cell.
 7. The process of claim 1,further comprising introducing catalyst additives to the electrolyte andthereby contributing to kinetics of the mediated electrochemicalprocesses while keeping the additives from becoming directly involved inthe oxidizing Sharps I and sterilizing Sharps II and biological wastematerials.
 8. The process of claim 1, further comprising addingstabilizing compounds to the electrolyte for overcoming and stabilizingthe short lifetime of oxidized forms of higher oxidation state speciesof the mediator.
 9. The process of claim 1, wherein the oxidizingspecies are identified in Table I, and wherein each of the species hasnormal valence states and higher valence oxidizing states and furthercomprising creating the higher valence oxidizing states of the oxidizingspecies by stripping electrons from normal valence state species in theelectrochemical cell.
 10. The process of claim 1, wherein the oxidizingspecies are super oxidizers which exhibit oxidation potentials of atleast 1.7 volts at 1 molar, 25° C. and pH1 and which are redox couplespecies that have the capability of producing free radicals of hydroxylor perhydroxyl, and further comprising creating free radical secondaryoxidizers by reacting the super oxidizers with water.
 11. The process ofclaim 1, further comprising using an alkaline solution, aidingdecomposing of the biological materials derived from base promoted esterhydrolysis, saponification, of fatty acids, and forming water solublealkali metal salts of the fatty acids and glycerin in a process similarto the production of soap from animal fat by introducing it into a hotaqueous lye solution.
 12. The process of claim 1, further comprisingusing an alkaline anolyte solution for absorbing CO₂ from the oxidizingSharps I and sterilizing Sharps II and biological waste materials andforming bicarbonate/carbonate solutions, which subsequently circulatethrough the electrochemical cell, producing percarbonate oxidizers. 13.The process of claim 1, wherein the oxidizing agents are superoxidizers, and further comprising generating inorganic free radicals inaqueous solutions from carbonate, azide, nitrite, nitrate, phosphite,phosphate, sulfite, sulfate, selenite, thiocyanate, chloride, bromide,iodide, and formate oxidizing species.
 14. The process of claim 1,wherein the membrane is microporous plastic, ion-selective, porousceramic or sintered glass frit.
 15. The process of claim 1, furthercomprising impressing an AC voltage upon the direct current voltage forretarding formation of cell performance limiting surface films on theelectrode.
 16. The process of claim 1, further comprising disposing aforaminous basket in the anolyte and holding the materials in thebasket.
 17. The process of claim 1, wherein the catholyte contains HNO₃or NO₃ ⁻ salts, and further comprising adding oxygen to the catholyteportion.
 18. The process of claim 1, wherein the mediator is simpleanions described in Table I, Type I isopolyanions containing tungsten,molybdenum, vanadium, niobium, tantalum, or combinations thereof asaddenda atoms; Type I heteropolyanions formed by incorporation into theaforementioned isopolyanions, as heteroatoms, any of the elements listedin Table II, either singly or in combinations thereof; or anyheteropolyanions containing at least one heteroatom type contained inboth Table I and Table II.
 19. The process of claim 1, furthercomprising adjusting temperature between 0° C. and temperature of theanolyte portion before it enters the electrochemical cell for enhancinggeneration of oxidized forms of the mediator, and adjusting thetemperature between 0° C. and below the boiling temperature of theanolyte portion entering the anolyte reaction chamber affecting desiredchemical reactions at desired rates.
 20. The process of claim 1, furthercomprising introducing an ultrasonic energy into the anolyte portion,rupturing cell membranes in the biological materials by momentarilyraising local temperature within the cell membranes with the ultrasonicenergy to above several thousand degrees, and causing cell membranefailure.
 21. The process of claim 1, further comprising the evolving ofoxygen from the anode is feed to a hydrogen fuel apparatus to increasethe percentage oxygen available from the ambient air.
 22. The process ofclaim 1, further comprising introducing ultraviolet energy into theanolyte portion and decomposing hydrogen peroxide and ozone intohydroxyl free radicals therein, thereby increasing efficiency of theprocess by converting products of electron consuming parasiticreactions, ozone and hydrogen peroxide, into viable free radicalsecondary oxidizers without consumption of additional electrons.
 23. Theprocess of claim 1, further comprising adding a surfactant to theanolyte portion for promoting dispersion of the materials orintermediate stage reaction products within the aqueous solution whenthe materials or reaction products are not water-soluble and tend toform immiscible layers.
 24. The process of claim 1, further comprisingattacking specific organic molecules with the oxidizing species whileoperating at low temperatures and preventing formation of dioxins andfurans.
 25. The process of claim 1, further comprising breaking down thebiological materials on Sharps I and II into biological and organiccompounds and attacking these compounds using as the mediator simpleand/or complex anion redox couple mediators or inorganic free radicalsand generating organic free radicals.
 26. The process of claim 1,wherein the treating and oxidizing Sharps I and sterilizing Sharps IIand biological and organic waste materials comprises treating andoxidizing Sharps I and sterilizing Sharps II and biological wastematerials.
 27. The process of claim 1, further comprising raising normalvalence state mediator anions to a higher valence state by stripping themediator anions of electrons in the electrochemical cell, whereinoxidized forms of weaker redox couples present in the mediator areproduced by similar anodic oxidation or reaction with oxidized forms ofstronger redox couples present and the oxidized species of the redoxcouples oxidize molecules of the materials and are themselves convertedto their reduced form, whereupon they are oxidized by the aforementionedmechanisms and the redox cycle continues.
 28. A process for treating andoxidizing Sharps I into metallic ions in solution in the anolyte andsterilizing Sharps II and destroying biological and organic wastematerials, comprising circulating anions of mediator oxidizing speciesin an electrolyte through an electrochemical cell and affecting anodicoxidation of reduced forms of reversible redox couples into oxidizedforms, contacting the anions with the organic waste in an anolyteportion of the electrolyte in a primary oxidation process, involvingsuper oxidizer anions, having an oxidation potential above a thresholdvalue of 1.7 volts at 1 molar, 25° C. and pH1 are present there is afree radical oxidizer driven secondary oxidation process, adding energyfrom an energy source to the anolyte portion and augmenting thesecondary oxidation processes, breaking down hydrogen peroxide and ozonein the anolyte portion into hydroxyl free radicals, and increasing anoxidizing effect of the secondary oxidation processes.
 29. The processof claim 28, wherein the adding energy comprises irradiating the anolyteportion with ultraviolet energy.
 30. The process of claim 28, whereinthe adding energy comprises introducing an ultrasonic energy source intothe anolyte portion, irradiating cell membranes in the organic waste,momentarily raising local temperature within the cell membranes, causingcell membrane failure, and creating greater exposure of cell contents tooxidizing species in the anolyte portion.
 31. The process of claim 28,wherein the mediator oxidizing species are simple anions redox couplemediators described in Table I; Type I isopolyanions formed by Mo, W, V,Nb, Ta, or mixtures thereof; Type I heteropolyanions formed byincorporation into the isopolyanions if any of the elements listed inTable II (heteroatoms) either singly or in thereof, or heteropolyanionscontaining at least one heteroatom type element contained in both TableI and Table II or combinations of the mediator oxidizing species fromany or all of these generic groups.
 32. The process of claim 28, furthercomprising using oxidizer species that are found in situ in the waste tobe decomposed, by circulating the waste-anolyte mixture through theelectrochemical cell where in an oxidized form of an in situ reversibleredox couple is formed by anodic oxidizing or reacting with an oxidizedform of a more powerful redox couple added to the anolyte and anodicallyoxidized in the electrochemical cell, thereby destroying the biologicalwaste materials, oxidizing Sharps I into metallic ions in solution inthe anolyte and sterilizing Sharps II.
 33. The process of claim 28,further comprising using an alkaline electrolyte selected from a groupconsisting of NaOH or KOH and combinations thereof, with the mediatoroxidizing species, wherein a reduced form of a mediator redox couple hassufficient solubility in said electrolyte for allowing desired oxidationof Sharps I and sterilizing Sharps II and destroying biological andorganic waste materials.
 34. The process of claim 28, wherein theoxidation potential of redox reactions of the mediator oxidizing speciesand the biological and organic waste molecules producing hydrogen ionsare inversely proportional to electrolyte pH, and thus with a selectionof a mediator redox couple increasing the electrolyte pH reduces theelectric potential required, thereby reducing electric power consumedper unit mass of the biological and organic waste destroyed.
 35. Theprocess of claim 28, wherein the electrolyte is an aqueous solutionchosen from acids, alkalines and neutral electrolytes and mixturesthereof.
 36. The process of claim 28, wherein the adding energycomprises using ultrasonic energy and inducing microscopic bubbleexpansion and implosion for reducing size of waste volumes dispersed inthe anolyte.
 37. The process of claim 28, further comprisinginterchanging the mediator oxidizing species without changing equipment,and wherein the electrolyte is an acid, neutral or alkaline aqueoussolution.
 38. The process of claim 28, wherein the treating andoxidizing Sharps I into metallic ions in solution in the anolyte andsterilizing Sharps II and destroying biological and organic wastematerials comprises treating and oxidizing waste from military ships,submarines, destroyers, cruisers and carriers.
 39. The process of claim28, wherein the treating and Sharps I into metallic ions in solution inthe anolyte and sterilizing Sharps II and destroying biological andorganic waste materials comprises treating and oxidizing waste fromcommercial ships, cruise ships, tankers, cargo ships, fishing boats,recreational craft and houseboats.
 40. The process of claim 28, furthercomprising separating the anolyte portion and a catholyte portion of theelectrolyte with a hydrogen or hydronium ion-permeable membrane,microporous polymer, porous ceramic or glass frit membrane.
 41. Theprocess of claim 28, further comprising electrically energizing theelectrochemical cell at a potential level sufficient for forming theoxidized forms of redox couples having highest oxidizing potential inthe anolyte, introducing the organic waste into the anolyte portion,forming reduced forms of one or more reversible redox couples bycontacting with oxidizable molecules, the reaction with which oxidizesthe oxidizable material with the concomitant reduction of the oxidizedform of the reversible redox couples to their reduced form, and whereinthe adding energy comprises providing an ultrasonic source connected tothe anolyte for augmenting secondary oxidation processes by momentarilyheating the hydrogen peroxide in the electrolyte to 4800° C. at 1000atmospheres thereby dissociating the hydrogen peroxide into hydroxylfree radicals thus increasing the oxidizing processes.
 42. The processof claim 41, further comprising oxidation potentials of redox reactionsproducing hydrogen ions are inversely related to pH;
 43. The process ofclaim 28, wherein the process is performed at a temperature fromslightly above 0° C. to slightly below the boiling point of theelectrolyte.
 44. The process of claim 43, wherein the temperature atwhich the process is performed is varied.
 45. The process of claim 28,wherein the treating and Sharps I into metallic ions in solution in theanolyte and sterilizing Sharps II and destroying biological and organicwaste materials comprises treating and oxidizing solid waste.
 46. Theprocess of claim 28, wherein the treating and Sharps I into metallicions in solution in the anolyte and sterilizing Sharps II and destroyingbiological and organic waste materials comprises treating and oxidizingliquid waste.
 47. The process of claim 28, wherein the treating andSharps I into metallic ions in solution in the anolyte and sterilizingSharps II and destroying biological and organic waste materialscomprises treating and oxidizing a combination of liquids and solids.48. The process of claim 28, further comprising requiring removing andtreating precipitates resulting from combinations of the oxidizingspecies and other species released from the biological and organic wasteduring destruction and sterilization.
 49. The process of claim 28,further comprising a catholyte portion of the electrolyte, and whereinthe anolyte and catholyte portions of electrolyte are independent of oneanother, and comprise aqueous solutions of acids, alkali or neutralsalt.
 50. The process of claim 28, further comprising separating acatholyte portion of the electrolyte from the anolyte portion with amembrane, operating the electrochemical cell at a current densitygreater then 0.5 amp per square centimeter across the membrane, and neara limit over which there is the possibility that metallic anions mayleak through the membrane in small quantities, and recovering themetallic anions through a resin column, thus allowing a greater rate ofdestruction of materials in the anolyte portion.
 51. The process ofclaim 28, wherein the catholyte solution further comprises an aqueoussolution and the electrolyte in the solution is composed of acids,alkali or neutral salts of strong acids and bases, and furthercomprising adding oxygen to this solution when HNO₃ or NO₃ ⁻ can occurin the catholyte, controlling concentration of electrolyte in thecatholyte to maintain conductivity of the catholyte portion desired inthe electrochemical cell, providing mechanical mixing and/or ultrasonicenergy induced microscopic bubble formation, and implosion for vigorousmixing in the catholyte solution for oxidizing the nitrous acid andsmall amounts of nitrogen oxides NO_(x), introducing air into thecatholyte portion for promoting the oxidizing of the nitrous acid andthe small amounts of N_(x), and diluting any hydrogen produced in thecatholyte portion before releasing the air and hydrogen.
 52. The processof claim 28, further comprising the evolving of hydrogen is feed to anapparatus that use hydrogen as a fuel (e.g., a fuel cell or a hydrogenburner).
 53. Apparatus for treating and oxidizing Sharps I into metallicions in solution in the anolyte and sterilizing Sharps II and destroyingbiological and organic waste materials comprising an electrochemicalcell, an aqueous electrolyte disposed in the electrochemical cell, ahydrogen or hydronium ion-permeable or selective membrane, disposed inthe electrochemical cell for separating the cell into anolyte andcatholyte chambers and separating the electrolyte into aqueous anolyteand catholyte portions, electrodes further comprising an anode and acathode disposed in the electrochemical cell respectively in the anolyteand catholyte chambers and in the anolyte and catholyte portions of theelectrolyte, a power supply connected to the anode and the cathode forapplying a direct current voltage between the anolyte and the catholyteportions of the electrolyte, and oxidizing of the materials in theanolyte portion with a mediated electrochemical oxidation (MEO) processwherein the anolyte portion further comprises a mediator in aqueoussolution for producing reversible redox couples used as oxidizingspecies and the electrolyte is an acid, neutral or alkaline aqueoussolution.
 54. The apparatus of claim 53, further comprising an anolytereaction chamber and buffer tank housing the bulk of the anolytesolution, an input pump to enter liquid animal waste into the anolytereaction chamber, a spray head and stream head to introduce the anolytefrom the electrochemical cell into the anolyte reaction chamber in sucha manner as to promote mixing of the incoming anolyte and the anolytemixture in the anolyte reaction chamber, a hinged lib to allow insertionof waste into the anolyte portion as liquid, solid of combination ofboth, a locking latch to secure the lid during operation of the system,a suction pump attached to the buffer tank to pump anolyte from thebuffer tank to the anolyte reaction chamber, a input pump to pumpanolyte from the anolyte reaction chamber back to the buffer tank, andan air pump to pump off gases from the anolyte reaction chamber back tothe buffer tank for further oxidation.
 55. The apparatus of claim 53,further comprising a foraminous basket disposed in the anolyte chamberfor receiving the Sharps I and II materials.
 56. The apparatus of claim53, further comprising additives disposed in the electrolyte forcontributing to kinetics of the mediated electrochemical processes whilekeeping it from becoming directly involved in the oxidizing of thematerials, and stabilizer compounds disposed in the electrolyte forstabilizing higher oxidation state species of oxidized forms of thereversible redox couples used as the oxidizing species in theelectrolyte.
 57. The apparatus of claim 53, wherein the oxidizer speciesare simple anions redox couple mediators described in Table I: Type Iisopolyanions formed by Mo, W, V, Nb, Ta, or mixtures there of, Type Iheteropolyanions formed by incorporation into the isopolyanions inheteroatom elements listed in Table II, or any heteropolyanionscontaining at least one heteroatom type element contained in both TableI and Table II or combinations of mediator species from any or all ofthese generic groups.
 58. The apparatus of claim 53, wherein theoxidizing species are super oxidizers and further comprising creatingsecondary oxidizers disposed in the anolyte portion by reacting with thesuper oxidizers in the aqueous anolyte.
 59. The apparatus of claim 53,wherein the anolyte portion comprises an alkaline solution for aidingdecomposing the materials, for absorbing CO₂, for forming alkali metalbicarbonate/carbonate for circulating through the electrochemical cell,and for producing a percarbonate oxidizer.
 60. The apparatus of claim53, wherein the anolyte portion further comprises super oxidizersgenerating inorganic free radicals in aqueous solutions derived fromcarbonate, azide, nitrite, nitrate, phosphite, phosphate, sulfite,sulfate, selenite, thiocyanate, chloride, bromide, and iodide species,anions with an oxidation potential above a threshold value of 1.7 voltsat 1 molar, 25° C. and pH1 (i.e., super oxidizer) for involving in asecondary oxidation process for producing oxidizers, and organic freeradicals for aiding the process and breaking down Sharps I into metallicions in solution in the anolyte and the biological and organic materialsinvolved with Sharps II and III into simpler smaller molecular structurebiological and organic compounds.
 61. The apparatus of claim 53, furthercomprising an ultrasonic energy source within or near the anolytechamber for producing microscopic bubbles and implosions for reducing insize individual second phase waste volumes dispersed in the anolyte. 62.The apparatus of claim 53, wherein the membrane is made of microporouspolymer, porous ceramic or glass frit.
 63. The apparatus of claim 53,further comprising an AC source for impression of an AC voltage upon theDC voltage to retard the formation of cell performance limiting surfacefilms on the electrodes.
 64. The apparatus of claim 53, furthercomprising an air sparge connected to the catholyte reservoir, wherebyoxygen contained in the air oxidizes nitrous acid and the small amountsof nitrogen oxides (NO_(x)), produced by cathode reactions when HNO₃ orNO₃ ⁻ salts are present in the catholyte.
 65. The apparatus of claim 53,wherein each of the oxidizing species has normal valence states inreduced forms of redox couples and higher valence oxidizing statesoxidized forms of redox couples of the oxidizing species created bystripping and reducing electrons off normal valence state species in theelectrochemical cell.
 66. The apparatus of claim 53, wherein the anolyteportions are alkaline solutions and oxidation potentials of redoxreactions producing hydrogen ions are inversely related to pH, whichreduces the electrical power required to oxidize Sharps I into metallicions in solution in the anolyte and sterilizing Sharps II and destroyingthe biological and organic waste.
 67. The apparatus of claim 53, whereinthe oxidizing species attack specific organic molecules while operatingat temperatures sufficiently low so as to preventing the formation ofdioxins and furans.
 68. The apparatus of claim 53, wherein the powersupply energizes the electrochemical cell at a potential levelsufficient to form the oxidized form of the redox couple having thehighest oxidation potential in the anolyte, and further comprising aheat exchanger connected to the anolyte chamber for controllingtemperature between 0° C. and slightly below the boiling temperature ofthe anolyte with the heat exchanger before the anolyte enters theelectrochemical cell enhancing the generation of oxidized forms of theanion redox couple mediator, and adjusting the temperature of theanolyte to the range between 0° C. and slightly below the boilingtemperature when entering the anolyte reaction chamber.
 69. Theapparatus of claim 53, wherein the oxidizing species are one or moreType I isopolyanion complex anion redox couple mediators containingtungsten, molybdenum, vanadium, niobium, tantalum, or combinationsthereof as addenda atoms in aqueous solution;
 70. The apparatus of claim69, wherein the oxidizing species are one or more Type Iheteropolyanions formed by incorporation into the isopolyanions, asheteroatoms, of the elements listed in Table II, either singly or incombination thereof.
 71. The apparatus of claim 53, wherein theoxidizing species are one or more heteropolyanions containing at leastone heteroatom type element contained in Table I and Table II.
 72. Theapparatus of claim 53, wherein the oxidizing species are higher valencestate of species found in situ for destroying of Sharps I into metallicions in solution in the anolyte and the sterilizing of Sharps and thedestroying of biological and organic waste materials.
 73. The apparatusof claim 53, wherein the waste material contains pharmaceuticalmaterials in the biological and organic materials on the Sharps I andII.
 74. The apparatus of claim 53, wherein the membrane is hydrogen orhydronium ion semi permeable or ion-selective, microporous polymer,porous ceramic or glass frit membrane for separating the anolyte portionand the catholyte portion while allowing hydrogen or hydronium ionpassage from the anolyte to the catholyte.
 75. The apparatus of claim53, wherein oxidation potentials of redox reactions producing hydrogenions are inversely related to pH, the biological and organic waste isliquid or solid, or a combination of liquids and solids, and theoxidizing species are interchangeable without changing other elements ofthe apparatus.
 76. The apparatus of claim 53, further comprising anultraviolet source connected to the anolyte chamber for decomposinghydrogen peroxide and ozone into hydroxyl free radicals as secondaryoxidizers and increasing efficiency of the process by recovering energythrough the oxidation of the materials in the anolyte chamber by thesecondary oxidizers.
 77. The apparatus of claim 53, further comprisingan ultrasonic source connected to the anolyte for augmenting secondaryoxidation processes by heating hydrogen peroxide containing electrolyteto 4800° C., at 1000 atmospheres for dissociating hydrogen-peroxide intohydroxyl free radicals and thus increasing concentration of oxidizingspecies and rate of waste destruction and for irradiating cell membranesin biological materials to momentarily raise the temperature within thecell membranes to above several thousand degrees, causing cell membranefailure, and creating greater exposure of cell contents to oxidizingspecies in the anolyte.
 78. The apparatus of claim 53, furthercomprising use of ultrasonic energy, via the ultrasonic energy sourcecommunicating with the anolyte for inducing microscopic bubbleimplosions to affect a reduction in size of the individual second phasewaste volumes dispersed in the anolyte.
 79. The apparatus of claim 53,further comprising an anolyte reaction chamber holding most of theanolyte portion and a foraminous basket, a penetrator attached to thebasket to puncture solids increasing the exposed area, and furthercomprising an external CO₂ vent connected to the reaction chamber forreleasing CO₂ into the atmosphere, a hinged lid attached to the reactionchamber allowing insertion of waste into the anolyte portion as liquid,solid, or mixtures of liquids and solids, an anolyte pump connected tothe reaction chamber, an inorganic compounds removal and treatmentsystem connected to the anolyte pump for removing chlorides, and otherprecipitate forming anions present in the biological and organic wastebeing processed, thereby precluding formation of unstable oxycompounds.80. The apparatus of claim 79, further comprising an off-gas cleaningsystem, comprising scrubber/absorption columns connected to the vent, acondenser connected to the anolyte reaction chamber, wherebynon-condensable incomplete oxidation products, low molecular weightorganics and carbon monoxide are reduced to acceptable levels foratmospheric release by the gas cleaning system, and wherein the anolyteoff-gas is contacted in the gas cleaning system wherein thenoncondensibles from the condenser are introduced into the lower portionof the gas cleaning system through a flow distribution system and asmall side stream of freshly oxidized anolyte direct from theelectrochemical cell is introduced into the upper portion of the column,resulting in a gas phase continuously reacting with the oxidizingmediator species as it rises up the column past the down flowinganolyte, and external drain, for draining to an organic compound removalsystem and the inorganic compounds removal and treatment system, and fordraining the anolyte system, wherein the organic compounds recoverysystem is used to recover biological materials that are benign and donot need further treatment, and biological materials that will be usedin the form they have been reduced.
 81. The apparatus of claim 79,further comprising thermal control units connected to heat or cool theanolyte to a selected temperature range when anolyte is circulated intothe reaction chamber through the electrochemical cell by pump on theanode chamber side of the membrane, a flush for flushing the anolyte,and a filter is located at the base of the reaction chamber to limit thesize of exiting solid particles to approximately 1 mm in diameter. 82.The apparatus of claim 53, wherein the direct current for theelectrochemical cell is provided by a DC power supply, which is poweredby an AC power supply, and wherein the DC power supply is low voltagehigh current supply operating at or below 10V DC and the AC power supplyoperates off an about 110v AC line for the smaller units and about 240vAC for larger units.
 83. The apparatus of claim 53, further comprisingan electrolyte containment boundary composed of materials resistant tothe oxidizing electrolyte selected from a group consisting of stainlesssteel, PTFE, PTFE lined tubing, glass and ceramics, and combinationsthereof.
 84. The apparatus of claim 53, further comprising an anolyterecovery system connected to a catholyte pump, a catholyte reservoirconnected to the cathode portion of the electrochemical cell, a thermalcontrol unit connected to the catholyte reservoir for varying thetemperature of the catholyte portion, a bulk of the catholyte portionbeing resident in a catholyte reservoir, wherein the catholyte portionof the electrolyte flows into a catholyte reservoir, and furthercomprising an air sparge connected to the catholyte reservoir forintroducing air into the catholyte reservoir.
 85. The apparatus of claim84, further comprising an anolyte recovery system for capturing theanions and for reintroducing the anions into the anolyte chamber uponcollection from the catholyte electrolyte, an off-gas cleaning systemconnected to the catholyte reservoir for cleaning gases before releaseinto the atmosphere, and an atmospheric vent connected to the off-gascleaning system for releasing gases into the atmosphere, wherein cleanedgas from the off-gas cleaning system is combined with unreactedcomponents of the air introduced into the system and discharged throughthe atmospheric vent
 47. 86. The apparatus of claim 84, furthercomprising a screwed top on the catholyte reservoir to facilitateflushing out the catholyte reservoir, a mixer connected to the catholytereservoir for stirring the catholyte, a catholyte pump connected to thecatholyte reservoir for circulating catholyte back to theelectrochemical cell, a drain for draining catholyte, a flush forflushing the catholyte system, and an air sparge connected to thehousing for introducing air into the catholyte reservoir, wherein thecatholyte portion of the electrolyte is circulated by pump through theelectrochemical cell on the cathode side of the membrane, and whereincontact of oxidizing gas with the catholyte portion of the electrolyteis enhanced by promoting gas/liquid contact by mechanical and/orultrasonic mixing.
 87. The apparatus of claim 53, wherein theelectrochemical cell is operated at high membrane current densitiesabove about 0.5 amps/cm² for increasing a rate of waste destruction,also results in increased mediator ion transport through the membraneinto the catholyte, and further comprising an anolyte recovery systempositioned on the catholyte side, air sparging on the catholyte side todilute and remove off-gas and hydrogen, wherein some mediator oxidizerions cross the membrane and are removed through the anolyte recoverysystem to maintain process efficiency or cell operability.
 88. Theapparatus of claim 53, further comprising a controller, amicroprocessor, a monitor and a keyboard connected to the cell forinputting commands to the controller through the keyboard responding tothe information displayed on the monitor, a program in the controllersequencing the steps for operation of the apparatus, program havingpre-programmed sequences of operations the operator follows or choosesother sequences of operations, the controller allows the operator toselect sequences within limits that assure a safe and reliableoperation, the controller sends digital commands that regulateelectrical power to pumps, mixers, thermal controls, ultravioletsources, ultrasonic sources, CO₂ vents, air sparge, and theelectrochemical cell, the controller receives component response andstatus from the components, the controller sends digital commands to thesensors to access sensor information through sensor responses, sensorsin the apparatus provide digital information on the state of components,sensors measure flow rate, temperature, pH, CO₂ venting, degree ofoxidation, and air sparging, the controller receives status informationon electrical potential across the electrochemical cell or individualcells in a multi-cell configuration and between the anodes and referenceelectrodes internal to the cells and the current flowing between theelectrodes within each cell.
 89. A organic waste destruction system,comprising a housing constructed of metal or high strength plasticsurrounding an electrochemical cell, with electrolyte and a foraminousbasket, an AC power supply with a power cord, a DC power supplyconnected to the AC power supply, the DC power supply providing directcurrent to the electrochemical cell, a control keyboard for input ofcommands and data, a monitor screen to display the systems operation andfunctions, an anolyte reaction chamber with a basket, status lights fordisplaying information about the status of the treatment of the organicwaste material, an air sparge for introducing air into a catholytereservoir below a surface of a catholyte, a CO₂ vent incorporated intothe housing to allow for CO₂ release from the anolyte reaction chamber,an atmospheric vent facilitating the releases of gases into theatmosphere from the catholyte reservoir, a hinged lid for opening anddepositing the organic waste in the basket in the anolyte reactionchamber, a locking latch connected to the hinged lid, and in the anolytereaction chamber an aqueous acid, alkali, or neutral salt electrolyteand mediated oxidizer species solution in which an oxidizer form of amediator redox couple initially may be present or may be generatedelectrochemically after introduction of the waste and application of DCpower to the electrochemical cell.
 90. The system of claim 89, whereinthe waste is introduced when the anolyte is at room temperature,operating temperature or intermediate temperature, and the organic wastematerial is rapidly oxidized at temperatures below boiling point ofanolyte at ambient pressure, and further comprising a pump circulatingan anolyte portion of an electrolyte, an in-line filter preventing solidparticles large enough to clog electrochemical cell flow paths fromexiting the reaction chamber, an inorganic compound removal andtreatment system and drain outlets connected to the anolyte reactionchamber, whereby residue is pacified in the form of a salt and may beperiodically removed, and a removable top connected to a catholytereservoir allowing access to the reservoir for cleaning and maintenance.91. A organic waste oxidizing process, comprising an operator engagingan ‘ON’ button on a control keyboard, a system controller which containsa microprocessor, running a program and controlling a sequence ofoperations, a monitor screen displaying process steps in propersequence, status lights on the panel providing status of the process,opening a lid and placing the organic waste in a basket as a liquid,solid, or a mixture of liquids and solids, retaining a solid portion ofthe waste and flowing a liquid portion through the basket and into ananolyte reaction chamber, activating a locking latch after the waste isplaced in the basket, activating pumps which begins circulating theanolyte and a catholyte, once the circulating is established throughoutthe system, operating mixers, once flow is established, turning onthermal control units, and initiating anodic oxidation and electrolyteheating programs, energizing an electrochemical cell to electricpotential and current density determined by the controller program,using programmed electrical power and electrolyte temperature ramps formaintaining a predetermined waste destruction rate profile as arelatively constant reaction rate as more reactive waste components areoxidized, thus resulting in the remaining waste becoming less and lessreactive, thereby requiring more and more vigorous oxidizing conditions,activating ultrasonic and ultraviolet systems in the anolyte reactionchamber and catholyte reservoir, releasing CO₂ from the biological andorganic waste oxidizing process in the anolyte reaction chamber,activating air sparge and atmospheric vent in a catholyte system,monitoring progress of the process in the controller by cell voltagesand currents, monitoring CO₂, CO, and O₂ gas composition for CO₂, CO andoxygen content, decomposing the organic waste into water and CO₂, thelatter being discharged out of the CO₂ vent, air sparging drawing airinto a catholyte reservoir, and discharging excess air out of anatmospheric vent, determining with an oxidation sensor that desireddegree of waste destruction has been obtained, setting the system tostandby, and executing system shutdown using the controller keyboardsystem operator.
 92. The process of claim 91, further comprising placingthe system in a standby mode during the day and adding organic waste asit is generated throughout the day, placing the system in fullactivation during non-business hours, operating the system at lowtemperature and ambient atmospheric pressure and not generating toxiccompounds during the oxidation of Sharps I into metallic ions insolution in the anolyte and sterilizing of sharps II and the destroyingof the biological and organic waste, making the process indoorscompatible, scaling the system between units small enough for use by asingle practitioner and units large enough to replace hospitalincinerators, releasing CO₂ oxidation product from the anolyte systemout through the CO₂ vent, and venting off-gas products from thecatholyte reservoir through the atmospheric vent.
 93. The process ofclaim 91, further comprising introducing the waste into a roomtemperature or cooler system with little or none of the mediator redoxcouple in the oxidizer form, depending upon reaction kinetics, heat ofreaction and similar waste characteristics.